Methods for controlling molecular weight and molecular weight distribution

ABSTRACT

Methods for controlling or adjusting the molecular weight and molecular weight distribution of an olefin polymer, such as an ethylene polymer, using an alkylaluminum compound are disclosed. In addition to the alkylaluminum compound, the catalyst systems contain a half-metallocene titanium phosphinimide compound and an activator.

REFERENCE TO RELATED APPLICATION

This application is a continuation-in-part application of co-pending U.S. patent application Ser. No. 15/481,502, filed on Apr. 7, 2017, the disclosure of which is incorporated herein by reference in its entirety.

BACKGROUND OF THE INVENTION

Polyolefins such as high density polyethylene (HDPE) homopolymer and linear low density polyethylene (LLDPE) copolymer can be produced using various combinations of catalyst systems and polymerization processes. However, typically the transition metal component of the catalyst system in Ziegler-Natta, chromium, and metallocene based catalyst systems is selected to produce ethylene polymers with specific molecular weight and molecular weight distribution (MWD) characteristics.

It would be beneficial, instead, to control or adjust the molecular weight and molecular weight distribution with another component of the catalyst system, such as an alkylaluminum compound or co-catalyst. Accordingly, it is to this end that the present invention is principally directed.

SUMMARY OF THE INVENTION

This summary is provided to introduce a selection of concepts in a simplified form that are further described below in the detailed description. This summary is not intended to identify required or essential features of the claimed subject matter. Nor is this summary intended to be used to limit the scope of the claimed subject matter.

Various processes and methods related to the control of the molecular weight and the molecular weight distribution of an olefin polymer are disclosed herein. In one aspect of this invention, an olefin polymerization process is provided, and in this aspect, the olefin polymerization process can comprise (i) contacting a half-metallocene titanium phosphinimide compound and an alkylaluminum compound for a first period of time to form a precontacted mixture, (ii) contacting the precontacted mixture with an activator and an optional co-catalyst for a second period of time to form a catalyst composition, and (iii) contacting the catalyst composition with an olefin monomer and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce an olefin polymer. The molecular weight (i.e., Mw) of the olefin polymer can be increased by precontacting the half-metallocene titanium phosphinimide compound with the alkylaluminum compound, as compared to a catalyst system obtained by simultaneously combining the half-metallocene titanium phosphinimide compound, the alkylaluminum compound, the activator, and the co-catalyst (if used).

In accordance with another aspect of the present invention, a process for controlling the molecular weight distribution (i.e., the ratio of Mw/Mn) of an ethylene polymer is provided, and in this aspect, the process can comprises (A) contacting a catalyst composition with ethylene and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce the ethylene polymer, wherein the catalyst composition can comprise a half-metallocene titanium phosphinimide compound, an activator, and an alkylaluminum compound, and (B) adjusting a solubility parameter of the alkylaluminum compound to control the ratio of Mw/Mn of the ethylene polymer.

In yet another aspect of the invention, a process for producing an ethylene polymer with a target ratio of Mw/Mn is provided, and in this aspect, the process can comprise (a) selecting an alkylaluminum compound based on a solubility parameter of the alkylaluminum compound, and (b) contacting a catalyst composition with ethylene and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce the ethylene polymer with the target ratio of Mw/Mn. The catalyst composition can comprise a half-metallocene titanium phosphinimide compound, an activator, and the alkylaluminum compound.

Both the foregoing summary and the following detailed description provide examples and are explanatory only. Accordingly, the foregoing summary and the following detailed description should not be considered to be restrictive. Further, features or variations can be provided in addition to those set forth herein. For example, certain aspects can be directed to various feature combinations and sub-combinations described in the detailed description.

BRIEF DESCRIPTION OF THE FIGURES

FIG. 1 presents a plot of the molecular weight distributions of the copolymers of Examples 1-2.

FIG. 2 presents a plot of the molecular weight distributions of the copolymers of Examples 3-4.

FIG. 3 presents a plot of the molecular weight distributions of the copolymers of Examples 5-6.

FIG. 4 presents a plot of the molecular weight distributions of the copolymers of Examples 1 and 9.

FIG. 5 presents a plot of the molecular weight distributions of the copolymers of Examples 2 and 9.

FIG. 6 presents a plot of the molecular weight distributions of the copolymers of Examples 9-10.

FIG. 7 presents a plot of the molecular weight distributions of the copolymers of Examples 12-13.

FIG. 8 presents a plot of the molecular weight distributions of the copolymers of Examples 16-17.

FIG. 9 is a bar chart illustrating the impact of pre-contacting on the Mw of polymers produced using different alkylaluminum compounds.

FIG. 10 is a bar chart illustrating the ratio of Mw/Mn of polymers produced using different alkylaluminum compounds.

DEFINITIONS

To define more clearly the terms used herein, the following definitions are provided. Unless otherwise indicated, the following definitions are applicable to this disclosure. If a term is used in this disclosure but is not specifically defined herein, the definition from the IUPAC Compendium of Chemical Terminology, 2nd Ed (1997), can be applied, as long as that definition does not conflict with any other disclosure or definition applied herein, or render indefinite or non-enabled any claim to which that definition is applied. To the extent that any definition or usage provided by any document incorporated herein by reference conflicts with the definition or usage provided herein, the definition or usage provided herein controls.

Herein, features of the subject matter are described such that, within particular aspects, a combination of different features can be envisioned. For each and every aspect and each and every feature disclosed herein, all combinations that do not detrimentally affect the designs, compositions, processes, or methods described herein are contemplated with or without explicit description of the particular combination. Additionally, unless explicitly recited otherwise, any aspect or feature disclosed herein can be combined to describe inventive designs, compositions, processes, or methods consistent with the present disclosure.

While compositions and methods are described herein in terms of “comprising” various components or steps, the compositions and methods also can “consist essentially of” or “consist of” the various components or steps, unless stated otherwise. For example, a catalyst composition consistent with aspects of the present invention can comprise; alternatively, can consist essentially of; or alternatively, can consist of; a half-metallocene titanium phosphinimide compound, an activator, and an alkylaluminum compound.

The terms “a,” “an,” “the,” etc., are intended to include plural alternatives, e.g., at least one, unless otherwise specified. For instance, the disclosure of “an activator-support” or “a half-metallocene titanium phosphinimide” is meant to encompass one, or mixtures or combinations of more than one, activator-support or half-metallocene titanium phosphinimide compound, respectively, unless otherwise specified.

Generally, groups of elements are indicated using the numbering scheme indicated in the version of the periodic table of elements published in Chemical and Engineering News, 63(5), 27, 1985. In some instances, a group of elements can be indicated using a common name assigned to the group; for example, alkali metals for Group 1 elements, alkaline earth metals for Group 2 elements, transition metals for Group 3-12 elements, and halogens or halides for Group 17 elements.

For any compound(s) disclosed herein, the structure or name presented also is intended to encompass all structural isomers, conformational isomers, and stereoisomers that can arise from a particular set of substituents, or the binding of different enantiotopic faces of a cyclopentadienyl-type ligand (e.g., substituted cyclopentadienyl, indenyl, substituted fluorenyl, etc.) to a metal atom, unless indicated otherwise. Thus, a general reference to a compound includes all structural isomers unless explicitly indicated otherwise; e.g., a general reference to pentane includes n-pentane, 2-methyl-butane, and 2,2-dimethylpropane, while a general reference to a butyl group includes an n-butyl group, a sec-butyl group, an iso-butyl group, and a tert-butyl group. Additionally, the reference to a general or specific structure or name encompasses all enantiomers, diastereomers, and other optical isomers whether in enantiomeric or racemic forms, as well as mixtures of stereoisomers, as the context permits or requires.

Unless otherwise specified, the term “substituted” when used to describe a group, for example, when referring to a substituted analog of a particular group, is intended to describe any non-hydrogen moiety that formally replaces a hydrogen in that group, and is intended to be non-limiting. Also, unless otherwise specified, a group or groups can also be referred to herein as “unsubstituted” or by equivalent terms such as “non-substituted,” which refers to the original group in which a non-hydrogen moiety does not replace a hydrogen within that group. Moreover, unless otherwise specified, “substituted” is intended to be non-limiting and include inorganic substituents or organic substituents as understood by one of ordinary skill in the art.

The term “hydrocarbon” whenever used in this specification and claims refers to a compound containing only carbon and hydrogen, whether saturated or unsaturated. Other identifiers can be utilized to indicate the presence of particular groups in the hydrocarbon (e.g., halogenated hydrocarbon indicates the presence of one or more halogen atoms replacing an equivalent number of hydrogen atoms in the hydrocarbon). The term “hydrocarbyl group” is used herein in accordance with the definition specified by IUPAC: a univalent group formed by removing a hydrogen atom from a hydrocarbon (that is, a group containing only carbon and hydrogen). Non-limiting examples of hydrocarbyl groups include alkyl, alkenyl, aryl, and aralkyl groups, amongst other groups.

The term “polymer” is used herein generically to include olefin homopolymers, copolymers, terpolymers, and so forth, as well as alloys and blends thereof. The term “polymer” also includes all possible geometrical configurations, unless stated otherwise, and such configurations can include isotactic, syndiotactic, and random symmetries. The term “polymer” also includes impact, block, graft, random, and alternating copolymers. A copolymer is derived from an olefin monomer and one olefin comonomer, while a terpolymer is derived from an olefin monomer and two olefin comonomers. Accordingly, “polymer” encompasses copolymers, terpolymers, etc., derived from any olefin monomer and comonomer(s) disclosed herein. Similarly, an ethylene polymer would include ethylene homopolymers, ethylene copolymers, ethylene terpolymers, and the like. As an example, an olefin copolymer, such as an ethylene copolymer, can be derived from ethylene and a comonomer, such as 1-butene, 1-hexene, or 1-octene. If the monomer and comonomer were ethylene and 1-hexene, respectively, the resulting polymer can be categorized an as ethylene/1-hexene copolymer.

In like manner, the scope of the term “polymerization” includes homopolymerization, copolymerization, terpolymerization, etc. Therefore, a copolymerization process can involve contacting one olefin monomer (e.g., ethylene) and one olefin comonomer (e.g., 1-hexene) to produce a copolymer.

The term “co-catalyst” is used generally herein to refer to compounds such as aluminoxane compounds, organoboron or organoborate compounds, ionizing ionic compounds, organoaluminum compounds, organozinc compounds, organomagnesium compounds, organolithium compounds, and the like, that can constitute one component of a catalyst composition, when used, for example, in addition to an activator-support. The term “co-catalyst” is used regardless of the actual function of the compound or any chemical mechanism by which the compound may operate.

The term “activator-support” is used herein to indicate a solid, inorganic oxide of relatively high porosity, which can exhibit Lewis acidic or Brønsted acidic behavior, and which has been treated with an electron-withdrawing component, typically an anion, and which is calcined. The electron-withdrawing component is typically an electron-withdrawing anion source compound. Thus, the activator-support can comprise a calcined contact product of at least one solid oxide with at least one electron-withdrawing anion source compound. The terms “support” and “activator-support” are not used to imply these components are inert, and such components should not be construed as an inert component of the catalyst composition. The term “activator,” as used herein, refers generally to a substance that is capable of converting a half-metallocene titanium phosphinimide compound into a catalyst that can polymerize olefins, or converting a contact product of a half-metallocene titanium phosphinimide compound and a component that provides an activatable ligand (e.g., an alkyl, a hydride) to the half-metallocene titanium phosphinimide compound, when the half-metallocene titanium phosphinimide compound does not already comprise such a ligand, into a catalyst that can polymerize olefins. This term is used regardless of the actual activating mechanism. Illustrative activators include activator-supports, aluminoxanes, organoboron or organoborate compounds, ionizing ionic compounds, and the like. Aluminoxanes, organoboron or organoborate compounds, and ionizing ionic compounds generally are referred to as activators if used in a catalyst composition in which an activator-support is not present. If the catalyst composition contains an activator-support, then the aluminoxane, organoboron or organoborate, and ionizing ionic materials are typically referred to as co-catalysts.

The terms “catalyst composition,” “catalyst mixture,” “catalyst system,” and the like, do not depend upon the actual product or composition resulting from the contact or reaction of the initial components of the disclosed or claimed catalyst composition/mixture/system, the nature of the active catalytic site, or the fate of the co-catalyst, the half-metallocene titanium phosphinimide compound, or the activator (e.g., activator-support), after combining these components. Therefore, the terms “catalyst composition,” “catalyst mixture,” “catalyst system,” and the like, encompass the initial starting components of the composition, as well as whatever product(s) may result from contacting these initial starting components, and this is inclusive of both heterogeneous and homogenous catalyst systems or compositions. The terms “catalyst composition,” “catalyst mixture,” “catalyst system,” and the like, can be used interchangeably throughout this disclosure.

The term “contact product” is used herein to describe methods and compositions wherein the components are contacted together in any order, in any manner, and for any length of time, unless otherwise specified. For example, the components can be contacted by blending or mixing. Further, unless otherwise specified, the contacting of any component can occur in the presence or absence of any other component of the methods and compositions described herein. Combining additional materials or components can be done by any suitable method. This term encompasses mixtures, blends, solutions, slurries, reaction products, and the like, as well as combinations thereof. Although “contact product” can include reaction products, it is not required for the respective components to react with one another. Similarly, the term “contacting” is used herein to refer to materials which can be blended, mixed, slurried, dissolved, reacted, treated, or otherwise combined in some other manner.

The term “precontacted mixture” describes a mixture of catalyst components that are combined or contacted for a period of time prior to being contacted with other catalyst components. According to this description, it is possible for the components of the precontacted mixture, once contacted, to have reacted to form at least one chemical compound, formulation, species, or structure different from the distinct initial compounds or components used to prepare the precontacted mixture. Generally, the precontacting step occurs outside of the polymerization reactor, such as in a mix tank or a catalyst preparation vessel, which ultimately feeds to the polymerization reactor.

The terms Mn, Mw, and Mz, as used herein, are defined as follows: Mn: number-average molecular weight; Mw: weight-average molecular weight; Mz: z-average molecular weight. These values are determined by calculations on the basis of molecular weight distribution curves determined using gel permeation chromatography (GPC), also known as size-exclusion chromatography (SEC).

Although any methods, devices, and materials similar or equivalent to those described herein can be used in the practice or testing of the invention, the typical methods, devices and materials are herein described.

All publications and patents mentioned herein are incorporated herein by reference for the purpose of describing and disclosing, for example, the constructs and methodologies that are described in the publications, which might be used in connection with the presently described invention.

Several types of ranges are disclosed in the present invention. When a range of any type is disclosed or claimed, the intent is to disclose or claim individually each possible number that such a range could reasonably encompass, including end points of the range as well as any sub-ranges and combinations of sub-ranges encompassed therein. For example, when a chemical moiety having a certain number of carbon atoms is disclosed or claimed, the intent is to disclose or claim individually every possible number that such a range could encompass, consistent with the disclosure herein. For example, the disclosure that a moiety is a C₁ to C₁₈ hydrocarbyl group, or in alternative language, a hydrocarbyl group having from 1 to 18 carbon atoms, as used herein, refers to a moiety that can have 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, or 18 carbon atoms, as well as any range between these two numbers (for example, a C₁ to C₈ hydrocarbyl group), and also including any combination of ranges between these two numbers (for example, a C₂ to C₄ and a C₁₂ to C₁₆ hydrocarbyl group).

Similarly, another representative example follows for the ratio of Mw/Mn of an ethylene polymer consistent with aspects of this invention. By a disclosure that the ratio of Mw/Mn can be in a range from about 2 to about 18, the intent is to recite that the ratio of Mw/Mn can be any ratio in the range and, for example, can be equal to about 2, about 3, about 4, about 5, about 6, about 7, about 8, about 9, about 10, about 11, about 12, about 13, about 14, about 15, about 16, about 17, or about 18. Additionally, the ratio of Mw/Mn can be within any range from about 2 to about 18 (for example, from about 2 to about 10), and this also includes any combination of ranges between about 2 and about 18 (for example, the Mw/Mn ratio can be in a range from about 3 to about 5, or from about 7 to about 17). Likewise, all other ranges disclosed herein should be interpreted in a manner similar to these examples.

The term “about” means that amounts, sizes, formulations, parameters, and other quantities and characteristics are not and need not be exact, but can be approximate including being larger or smaller, as desired, reflecting tolerances, conversion factors, rounding off, measurement errors, and the like, and other factors known to those of skill in the art. In general, an amount, size, formulation, parameter or other quantity or characteristic is “about” or “approximate” whether or not expressly stated to be such. The term “about” also encompasses amounts that differ due to different equilibrium conditions for a composition resulting from a particular initial mixture. Whether or not modified by the term “about,” the claims include equivalents to the quantities. The term “about” can mean within 10% of the reported numerical value, preferably within 5% of the reported numerical value.

DETAILED DESCRIPTION OF THE INVENTION

Disclosed herein are processes and methods directed to controlling or adjusting the molecular weight or the molecular weight distribution of an olefin polymer, such as an ethylene polymer. For instance, it was surprisingly found that precontacting an alkylaluminum compound with a half-metallocene titanium phosphinimide compound during catalyst preparation, prior to olefin polymerization, can result in an increase in the molecular weight (Mw) of the polymer produced in the polymerization process. Further, it was surprisingly found that the selection of the alkylaluminum compound utilized in the catalyst system, and the respective solubility parameter of the alkylaluminum compound, can be used to adjust or control the molecular weight distribution (Mw/Mn) of the polymer.

Processes Relating to Molecular Weight

Consistent with aspects of this invention, an olefin polymerization process can comprise (i) contacting a half-metallocene titanium phosphinimide compound and an alkylaluminum compound for a first period of time to form a precontacted mixture, (ii) contacting the precontacted mixture with an activator and an optional co-catalyst for a second period of time to form a catalyst composition, and (iii) contacting the catalyst composition with an olefin monomer and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce an olefin polymer. The Mw of the olefin polymer produced by this process can be greater (by any amount disclosed herein) than the Mw of an olefin polymer produced under the same polymerization conditions using a catalyst system obtained by simultaneously combining the half-metallocene titanium phosphinimide compound, the alkylaluminum compound, the activator, and the optional co-catalyst. Thus, precontacting of the alkylaluminum compound and the half-metallocene titanium phosphinimide compound during catalyst preparation ultimately can result in an unexpected increase in the Mw of the polymer.

Generally, the features of any of the processes disclosed herein (e.g., the activator, the alkylaluminum compound, the half-metallocene compound, the first period of time, the olefin monomer and comonomer, and the Mw of the olefin polymer, among others) are independently described herein, and these features can be combined in any combination to further describe the disclosed processes. Moreover, other process steps can be conducted before, during, and/or after any of the steps listed in the disclosed processes, unless stated otherwise. Additionally, olefin polymers produced in accordance with the disclosed processes are within the scope of this disclosure and are encompassed herein.

Consistent with aspects of this invention, the Mw of the olefin polymer produced by the process can be greater than the Mw of an olefin polymer produced under the same polymerization conditions using a catalyst system obtained by simultaneously combining the half-metallocene titanium phosphinimide compound, the alkylaluminum compound, the activator, and the optional co-catalyst. In one aspect, the Mw of the olefin polymer produced by the process can be at least about 5% greater than the Mw of an olefin polymer produced under the same polymerization conditions using a catalyst system obtained by simultaneously combining the half-metallocene titanium phosphinimide compound, the alkylaluminum compound, the activator, and the optional co-catalyst, while in another aspect, the Mw of the olefin polymer produced by the process can be at least about 10% greater, at least about 15% greater, at least about 25%, and often up to 100-200% greater, than the Mw of an olefin polymer produced under the same polymerization conditions using a catalyst system obtained by simultaneously combining the half-metallocene titanium phosphinimide compound, the alkylaluminum compound, the activator, and the optional co-catalyst. Unexpectedly, the precontacting of the alkylaluminum compound and the half-metallocene titanium phosphinimide compound during catalyst preparation ultimately can result in an significant increase in the Mw of the polymer, when all other conditions are held constant.

The disclosed processes are applicable to any suitable half-metallocene titanium phosphinimide compound. In some aspects, the half-metallocene titanium phosphinimide compound can have the following formula:

Within formula (B), Cp, R¹, R², R³, X¹, and X² are independent elements of the half-metallocene titanium phosphinimide compound. Therefore, the half-metallocene titanium phosphinimide compound having formula (B) can be described using any combination of Cp, R¹, R², R³, X¹, and X² disclosed herein.

Unless otherwise specified, formula (B) above, any other structural formulas disclosed herein, and any half-metallocene titanium phosphinimide compound or species disclosed herein are not designed to show stereochemistry or isomeric positioning of the different moieties (e.g., these formulas are not intended to display rac or meso isomers, or R or S diastereoisomers), although such compounds are contemplated and encompassed by these formulas and/or structures, unless stated otherwise.

In accordance with aspects of this invention, X¹ and X² in formula (B) independently can be a halide (e.g., F, Cl, Br, etc.). It is contemplated that X¹ and X² can be either the same or a different halide. In some aspects, both X¹ and X² are Cl.

In formula (B), R¹, R², and R³ can be any suitable substituent. For instance, R¹, R², and R³ independently can be H or a halide, C₁ to C₃₆ hydrocarbyl group, C₁ to C₃₆ halogenated hydrocarbyl group, C₁ to C₃₆ hydrocarboxy group, or C₁ to C₃₆ hydrocarbylsilyl group. It is contemplated that R¹, R², and R³ can be the same or different. In one aspect, R¹, R², and R³ independently can be H, a halide, a C₁ to C₁₈ hydrocarbyl group, a C₁ to C₁₈ halogenated hydrocarbyl group, a C₁ to C₁₈ hydrocarboxy group, or a C₁ to C₁₈ hydrocarbylsilyl group. In another aspect, R¹, R², and R³ independently can be H, a halide, a C₁ to C₁₂ hydrocarbyl group, a C₁ to C₁₂ halogenated hydrocarbyl group, a C₁ to C₁₂ hydrocarboxy group, or a C₁ to C₁₂ hydrocarbylsilyl group. In yet another aspect, R¹, R², and R³ independently can be H, a halide, a C₁ to C₈ hydrocarbyl group, a C₁ to C₈ halogenated hydrocarbyl group, a C₁ to C₈ hydrocarboxy group, or a C₁ to C₈ hydrocarbylsilyl group.

R¹, R², and R³ independently can be H or a C₁ to C₁₈ hydrocarbyl group in certain aspects of this invention. For instance, R¹, R², and R³ in formula (B) independently can be a C₁ to C₁₈ alkyl group, a C₂ to C₁₈ alkenyl group, a C₄ to C₁₈ cycloalkyl group, a C₆ to C₁₈ aryl group, or a C₇ to C₁₈ aralkyl group; alternatively, R¹, R², and R³ independently can be a C₁ to C₁₂ alkyl group, a C₂ to C₁₂ alkenyl group, a C₄ to C₁₂ cycloalkyl group, a C₆ to C₁₂ aryl group, or a C₇ to C₁₂ aralkyl group; alternatively, R¹, R², and R³ independently can be a C₁ to C₁₀ alkyl group, a C₂ to C₁₀ alkenyl group, a C₄ to C₁₀ cycloalkyl group, a C₆ to C₁₀ aryl group, or a C₇ to C₁₀ aralkyl group; or alternatively, R¹, R², and R³ independently can be a C₁ to C₅ alkyl group, a C₂ to C₅ alkenyl group, a C₅ to C₈ cycloalkyl group, a C₆ to C₈ aryl group, or a C₇ to C₈ aralkyl group.

Accordingly, in some aspects, the alkyl group which can be any of R¹, R², and R³ in formula (B) can be a methyl group, an ethyl group, a propyl group, a butyl group, a pentyl group, a hexyl group, a heptyl group, an octyl group, a nonyl group, a decyl group, a undecyl group, a dodecyl group, a tridecyl group, a tetradecyl group, a pentadecyl group, a hexadecyl group, a heptadecyl group, or an octadecyl group; or alternatively, a methyl group, an ethyl group, a propyl group, a butyl group, a pentyl group, a hexyl group, a heptyl group, an octyl group, a nonyl group, or a decyl group. In some aspects, the alkyl group which can be any of R¹, R², and R³ in formula (B) can be a methyl group, an ethyl group, a n-propyl group, an iso-propyl group, a n-butyl group, an iso-butyl group, a sec-butyl group, a tert-butyl group, a n-pentyl group, an iso-pentyl group, a sec-pentyl group, or a neopentyl group; alternatively, a methyl group, an ethyl group, an iso-propyl group, a tert-butyl group, or a neopentyl group; alternatively, a methyl group; alternatively, an ethyl group; alternatively, a n-propyl group; alternatively, an iso-propyl group; alternatively, a tert-butyl group; or alternatively, a neopentyl group. Alternatively, R¹, R², and R³ independently can be a C₁ to C₈ alkyl group.

Suitable alkenyl groups which can be any of R¹, R², and R³ in formula (B) can include, but are not limited to, an ethenyl group, a propenyl group, a butenyl group, a pentenyl group, a hexenyl group, a heptenyl group, an octenyl group, a nonenyl group, a decenyl group, a undecenyl group, a dodecenyl group, a tridecenyl group, a tetradecenyl group, a pentadecenyl group, a hexadecenyl group, a heptadecenyl group, or an octadecenyl group. Such alkenyl groups can be linear or branched, and the double bond can be located anywhere in the chain. In one aspect, R¹, R², and R³ in formula (B) independently can be an ethenyl group, a propenyl group, a butenyl group, a pentenyl group, a hexenyl group, a heptenyl group, an octenyl group, a nonenyl group, or a decenyl group, while in another aspect, R¹, R², and R³ in formula (B) independently can be an ethenyl group, a propenyl group, a butenyl group, a pentenyl group, or a hexenyl group. For example, any of R¹, R², and R³ can be an ethenyl group; alternatively, a propenyl group; alternatively, a butenyl group; alternatively, a pentenyl group; or alternatively, a hexenyl group. In yet another aspect, any of R¹, R², and R³ can be a terminal alkenyl group, such as a C₃ to C₁₈ terminal alkenyl group, a C₃ to C₁₂ terminal alkenyl group, or a C₃ to C₈ terminal alkenyl group. For example, in some aspects, at least one of R¹, R², and R³ is a C₃ to C₁₂ alkenyl group, or a C₃ to C₁₂ terminal alkenyl group. Illustrative terminal alkenyl groups can include, but are not limited to, a prop-2-en-1-yl group, a bute-3-en-1-yl group, a pent-4-en-1-yl group, a hex-5-en-1-yl group, a hept-6-en-1-yl group, an octe-7-en-1-yl group, a non-8-en-1-yl group, a dece-9-en-1-yl group, and so forth.

Any of R¹, R², and R³ in formula (B) independently can be a cycloalkyl group, including, but not limited to, a cyclobutyl group, a substituted cyclobutyl group, a cyclopentyl group, a substituted cyclopentyl group, a cyclohexyl group, a substituted cyclohexyl group, a cycloheptyl group, a substituted cycloheptyl group, a cyclooctyl group, or a substituted cyclooctyl group. For example, any of R¹, R², and R³ in formula (B) can be a cyclopentyl group, a substituted cyclopentyl group, a cyclohexyl group, or a substituted cyclohexyl group. Moreover, R¹, R², and R³ in formula (B) independently can be a cyclobutyl group or a substituted cyclobutyl group; alternatively, a cyclopentyl group or a substituted cyclopentyl group; alternatively, a cyclohexyl group or a substituted cyclohexyl group; alternatively, a cycloheptyl group or a substituted cycloheptyl group; alternatively, a cyclooctyl group or a substituted cyclooctyl group; alternatively, a cyclopentyl group; alternatively, a substituted cyclopentyl group; alternatively, a cyclohexyl group; or alternatively, a substituted cyclohexyl group. Substituents which can be utilized for the substituted cycloalkyl group are independently disclosed herein and can be utilized without limitation to further describe the substituted cycloalkyl group which can be any of R¹, R², and R³ in formula (B).

In some aspects, the aryl group which can be any of R¹, R², and R³ in formula (B) can be a phenyl group, a substituted phenyl group, a naphthyl group, or a substituted naphthyl group. In an aspect, the aryl group can be a phenyl group or a substituted phenyl group; alternatively, a naphthyl group or a substituted naphthyl group; alternatively, a phenyl group or a naphthyl group; alternatively, a substituted phenyl group or a substituted naphthyl group; alternatively, a phenyl group; or alternatively, a naphthyl group. Substituents which can be utilized for the substituted phenyl groups or substituted naphthyl groups are independently disclosed herein and can be utilized without limitation to further describe the substituted phenyl groups or substituted naphthyl groups which can be any of R¹, R², and R³ in formula (B).

In an aspect, the substituted phenyl group which can be any of R¹, R², and R³ in formula (B) can be a 2-substituted phenyl group, a 3-substituted phenyl group, a 4-substituted phenyl group, a 2,4-disubstituted phenyl group, a 2,6-disubstituted phenyl group, a 3,5-disubstituted phenyl group, or a 2,4,6-trisubstituted phenyl group. In other aspects, the substituted phenyl group can be a 2-substituted phenyl group, a 4-substituted phenyl group, a 2,4-disubstituted phenyl group, or a 2,6-disubstituted phenyl group; alternatively, a 3-substituted phenyl group or a 3,5-disubstituted phenyl group; alternatively, a 2-substituted phenyl group or a 4-substituted phenyl group; alternatively, a 2,4-disubstituted phenyl group or a 2,6-disubstituted phenyl group; alternatively, a 2-substituted phenyl group; alternatively, a 3-substituted phenyl group; alternatively, a 4-substituted phenyl group; alternatively, a 2,4-disubstituted phenyl group; alternatively, a 2,6-disubstituted phenyl group; alternatively, a 3,5-disubstituted phenyl group; or alternatively, a 2,4,6-trisubstituted phenyl group. Substituents which can be utilized for these specific substituted phenyl groups are independently disclosed herein and can be utilized without limitation to further describe these substituted phenyl groups which can be any of R¹, R², and R³ in formula (B).

In some aspects, the aralkyl group which can be any of R¹, R², and R³ in formula (B) can be a benzyl group or a substituted benzyl group. In an aspect, the aralkyl group can be a benzyl group or, alternatively, a substituted benzyl group. Substituents which can be utilized for the substituted aralkyl group are independently disclosed herein and can be utilized without limitation to further describe the substituted aralkyl group which can be any of R¹, R², and R³ in formula (B).

In an aspect, each non-hydrogen substituent(s) for the substituted cycloalkyl group, substituted aryl group, or substituted aralkyl group which can be any of R¹, R², and R³ in formula (B) independently can be a C₁ to C₁₈ hydrocarbyl group; alternatively, a C₁ to C₈ hydrocarbyl group; or alternatively, a C₁ to C₅ hydrocarbyl group. Specific hydrocarbyl groups are independently disclosed herein and can be utilized without limitation to further describe the substituents of the substituted cycloalkyl groups, substituted aryl groups, or substituted aralkyl groups which can be any of R¹, R², and R³ in formula (B). For instance, the hydrocarbyl substituent can be an alkyl group, such as a methyl group, an ethyl group, a n-propyl group, an isopropyl group, a n-butyl group, a sec-butyl group, an isobutyl group, a tert-butyl group, a n-pentyl group, a 2-pentyl group, a 3-pentyl group, a 2-methyl-1-butyl group, a tert-pentyl group, a 3-methyl-1-butyl group, a 3-methyl-2-butyl group, or a neo-pentyl group, and the like. Furthermore, the hydrocarbyl substituent can be a benzyl group, a phenyl group, a tolyl group, or a xylyl group, and the like.

Any of R¹, R², and R³ in formula (B) independently can be, in certain aspects, a C₁ to C₃₆ halogenated hydrocarbyl group, where the halogenated hydrocarbyl group indicates the presence of one or more halogen atoms replacing an equivalent number of hydrogen atoms in the hydrocarbyl group. The halogenated hydrocarbyl group often can be a halogenated alkyl group, a halogenated alkenyl group, a halogenated cycloalkyl group, a halogenated aryl group, or a halogenated aralkyl group. Representative and non-limiting halogenated hydrocarbyl groups include pentafluorophenyl, trifluoromethyl (CF₃), and the like.

A hydrocarboxy group is used generically herein to include, for instance, alkoxy, aryloxy, aralkoxy, -(alkyl, aryl, or aralkyl)-O-(alkyl, aryl, or aralkyl) groups, and —O(CO)-(hydrogen or hydrocarbyl) groups, and these groups can comprise up to about 36 carbon atoms (e.g., C₁ to C₃₆, C₁ to C₁₈, C₁ to C₁₀, or C₁ to C₈ hydrocarboxy groups). Illustrative and non-limiting examples of hydrocarboxy groups which can be any of R¹, R², and R³ in formula (B) can include, but are not limited to, a methoxy group, an ethoxy group, an n-propoxy group, an isopropoxy group, an n-butoxy group, a sec-butoxy group, an isobutoxy group, a tert-butoxy group, an n-pentoxy group, a 2-pentoxy group, a 3-pentoxy group, a 2-methyl-1-butoxy group, a tert-pentoxy group, a 3-methyl-1-butoxy group, a 3-methyl-2-butoxy group, a neo-pentoxy group, a phenoxy group, a toloxy group, a xyloxy group, a 2,4,6-trimethylphenoxy group, a benzoxy group, an acetylacetonate group (acac), a formate group, an acetate group, a stearate group, an oleate group, a benzoate group, and the like. In an aspect, the hydrocarboxy group which can be any of R¹, R², and R³ in formula (B) can be a methoxy group; alternatively, an ethoxy group; alternatively, an n-propoxy group; alternatively, an isopropoxy group; alternatively, an n-butoxy group; alternatively, a sec-butoxy group; alternatively, an isobutoxy group; alternatively, a tert-butoxy group; alternatively, an n-pentoxy group; alternatively, a 2-pentoxy group; alternatively, a 3-pentoxy group; alternatively, a 2-methyl-1-butoxy group; alternatively, a tert-pentoxy group; alternatively, a 3-methyl-1-butoxy group, alternatively, a 3-methyl-2-butoxy group; alternatively, a neo-pentoxy group; alternatively, a phenoxy group; alternatively, a toloxy group; alternatively, a xyloxy group; alternatively, a 2,4,6-trimethylphenoxy group; alternatively, a benzoxy group; alternatively, an acetylacetonate group; alternatively, a formate group; alternatively, an acetate group; alternatively, a stearate group; alternatively, an oleate group; or alternatively, a benzoate group.

In accordance with some aspects disclosed herein, any of R¹, R², and R³ in formula (B) can be a C₁ to C₃₆ hydrocarbylsilyl group; alternatively, a C₁ to C₂₄ hydrocarbylsilyl group; alternatively, a C₁ to C₁₈ hydrocarbylsilyl group; or alternatively, a C₁ to C₈ hydrocarbylsilyl group. In an aspect, each hydrocarbyl (one or more) of the hydrocarbylsilyl group can be any hydrocarbyl group disclosed herein (e.g., a C₁ to C₅ alkyl group, a C₂ to C₅ alkenyl group, a C₅ to C₈ cycloalkyl group, a C₆ to C₈ aryl group, a C₇ to C₈ aralkyl group, etc.). As used herein, hydrocarbylsilyl is intended to cover (mono)hydrocarbylsilyl (—SiH₂R), dihydrocarbylsilyl (—SiHR₂), and trihydrocarbylsilyl (—SiR₃) groups, with R being a hydrocarbyl group. In one aspect, the hydrocarbylsilyl group can be a C₃ to C₃₆ or a C₃ to C₁₈ trihydrocarbylsilyl group, such as, for example, a trialkylsilyl group or a triphenylsilyl group. Illustrative and non-limiting examples of hydrocarbylsilyl groups which can be any of R¹, R², and R³ in formula (B) can include, but are not limited to, trimethylsilyl, triethylsilyl, tripropylsilyl (e.g., triisopropylsilyl), tributylsilyl, tripentylsilyl, triphenylsilyl, allyldimethylsilyl, and the like.

In some aspects, R¹, R², and R³ independently can be H, Cl, CF₃, a methyl group, an ethyl group, a propyl group, a butyl group (e.g., t-Bu), a pentyl group, a hexyl group, a heptyl group, an octyl group, a nonyl group, a decyl group, an ethenyl group, a propenyl group, a butenyl group, a pentenyl group, a hexenyl group, a heptenyl group, an octenyl group, a nonenyl group, a decenyl group, a phenyl group, a 2,6-diisopropylphenyl group, a tolyl group, a benzyl group, a naphthyl group, a trimethylsilyl group, a triisopropylsilyl group, a triphenylsilyl group, or an allyldimethylsilyl group.

Cp in formula (B) can be a substituted or unsubstituted cyclopentadienyl group, indenyl group, or fluorenyl group. Hence, Cp can be unsubstituted or can be substituted with any suitable substituent, any suitable number of substituents, and at any suitable position(s) that conforms to the rules of chemical valence. In one aspect, for instance, Cp can be a cyclopentadienyl group, while in another aspect, Cp can be an indenyl group, and in yet another aspect, Cp can be a fluorenyl group. In these and other aspects, Cp can be unsubstituted.

Alternatively, Cp can contain a substituent (one or more), such as H, a halide, a C₁ to C₃₆ hydrocarbyl group, a C₁ to C₃₆ halogenated hydrocarbyl group, a C₁ to C₃₆ hydrocarboxy group, or a C₁ to C₃₆ hydrocarbylsilyl group. The halide, C₁ to C₃₆ hydrocarbyl group, C₁ to C₃₆ halogenated hydrocarbyl group, C₁ to C₃₆ hydrocarboxy group, and C₁ to C₃₆ hydrocarbylsilyl group which can be a substituent on Cp in formula (B) can be any halide, C₁ to C₃₆ hydrocarbyl group, C₁ to C₃₆ halogenated hydrocarbyl group, C₁ to C₃₆ hydrocarboxy group, and C₁ to C₃₆ hydrocarbylsilyl group described herein (e.g., as pertaining to X¹, X², R¹, R², and/or R³ in formula (B)).

Thus, each substituent independently can be H; alternatively, a halide; alternatively, H or a C₁ to C₁₂ hydrocarbyl group; alternatively, a C₁ to C₁₂ halogenated hydrocarbyl group; alternatively, a C₁ to C₁₂ hydrocarboxy group; alternatively, a C₁ to C₁₂ hydrocarbylsilyl group; alternatively, a C₁ to C₁₂ hydrocarbyl group or a C₁ to C₁₂ hydrocarbylsilyl group; or alternatively, a C₁ to C₈ alkyl group or a C₃ to C₈ alkenyl group.

As a non-limiting example, each substituent on Cp independently can be H, Cl, CF₃, a methyl group, an ethyl group, a propyl group, a butyl group (e.g., t-Bu), a pentyl group, a hexyl group, a heptyl group, an octyl group, a nonyl group, a decyl group, an ethenyl group, a propenyl group, a butenyl group, a pentenyl group, a hexenyl group, a heptenyl group, an octenyl group, a nonenyl group, a decenyl group, a phenyl group, a tolyl group (or other substituted aryl group), a benzyl group, a naphthyl group, a trimethylsilyl group, a triisopropylsilyl group, a triphenylsilyl group, an allyldimethylsilyl group, or a 1-methylcyclohexyl group; alternatively, H; alternatively, Cl; alternatively, CF₃; alternatively, a methyl group; alternatively, an ethyl group; alternatively, a propyl group; alternatively, a butyl group; alternatively, a pentyl group; alternatively, a hexyl group; alternatively, a heptyl group; alternatively, an octyl group, a nonyl group; alternatively, a decyl group; alternatively, an ethenyl group; alternatively, a propenyl group; alternatively, a butenyl group; alternatively, a pentenyl group; alternatively, a hexenyl group; alternatively, a heptenyl group; alternatively, an octenyl group; alternatively, a nonenyl group; alternatively, a decenyl group; alternatively, a phenyl group; alternatively, a tolyl group; alternatively, a benzyl group; alternatively, a naphthyl group; alternatively, a trimethylsilyl group; alternatively, a triisopropylsilyl group; alternatively, a triphenylsilyl group; alternatively, an allyldimethylsilyl group; or alternatively, a 1-methylcyclohexyl group.

Illustrative and non-limiting examples of half-metallocene titanium phosphinimide compounds suitable for use in the processes disclosed herein can include the following compounds (tBu=tert-butyl; Ph=phenyl; Cy=cyclohexyl; iPr=isopropyl):

Consistent with step (i) of the processes disclosed herein, the half-metallocene titanium compound can be contacted (or reacted) with an alkylaluminum compound for a first period of time to form the precontacted mixture. In one aspect of this invention, the alkylaluminum compound can have the formula Al(R^(Z))₃. In this formula, each R^(Z) independently can be a C₁ to C₁₀ alkyl group; alternatively, a C₁ to C₈ alkyl group; alternatively, a C₁ to C₆ alkyl group; or alternatively, a C₁ to C₄ alkyl group. In an aspect, each R^(Z) independently can be a methyl group, an ethyl group, a propyl group, a butyl group (e.g., n-butyl or iso-butyl), a pentyl group, a hexyl group, a heptyl group, or an octyl group; alternatively, a methyl group, an ethyl group, a propyl group, a butyl group, a pentyl group, or a hexyl group; alternatively, a methyl group; alternatively, an ethyl group; alternatively, a propyl group; or alternatively, a butyl group.

For example, the alkylaluminum compound can comprise (or consist essentially of, or consist of) trimethylaluminum (TMA), triethylaluminum (TEA), tri-n-propylaluminum (TNPA), tri-n-butylaluminum (TNBA), triisobutylaluminum (TIBA), tri-n-hexylaluminum, tri-n-octylaluminum, and the like, or combinations thereof. In one aspect, the alkylaluminum compound can comprise (or consist essentially of, or consist of) trimethylaluminum, triethylaluminum, triisobutylaluminum, or a combination thereof. In another aspect, the alkylaluminum compound can comprise (or consist essentially of, or consist of) trimethylaluminum; alternatively, triethylaluminum; alternatively, tri-n-propylaluminum; alternatively, tri-n-butylaluminum; alternatively, triisobutylaluminum; alternatively, tri-n-hexylaluminum; or alternatively, tri-n-octylaluminum.

While not being limited thereto, the molar ratio (Al:Ti) of the alkylaluminum compound to the half-metallocene titanium compound in step (i) often can fall within a range of from about 0.5:1 to about 10:1. For instance, the minimum molar ratio of the alkylaluminum compound to the half-metallocene titanium compound can be about 0.5:1, about 0.8:1, about 0.9:1, about 1:1, about 1.1:1, about 1.2:1, or about 1.5:1; additionally or alternatively, the maximum molar ratio of the alkylaluminum compound to the half-metallocene titanium compound can be about 10:1, about 5:1, about 3:1, or about 2:1. Generally, the molar ratio of the alkylaluminum compound to the half-metallocene titanium compound in step (i) can be in a range from any minimum molar ratio disclosed herein to any maximum molar ratio disclosed herein. Therefore, suitable non-limiting ranges for the molar ratio of the alkylaluminum compound to the half-metallocene titanium compound can include the following ranges: from about 0.5:1 to about 10:1, from about 0.9:1 to about 10:1, from about 1:1 to about 5:1, from about 1.1:1 to about 3:1, or from about 1.1 to about 2:1. In some aspects, the molar ratio can be equal to about 1:1 (stoichiometric). Other appropriate ranges for the molar ratio of the alkylaluminum compound to the half-metallocene titanium compound in step (i) are readily apparent from this disclosure. If more than one alkylaluminum compound and/or more than one half-metallocene titanium compound is/are employed, this ratio is based on the total molar amounts of the respective components.

The contacting (or reacting) of the half-metallocene titanium phosphinimide compound having formula (B) with the alkylaluminum compound—also referred to herein as a precontacting step—to form the precontacted mixture is not limited to any particular temperature. Typically, however, the precontacting step and the formation of the precontacted mixture can be performed at a temperature in a range from about 0° C. to about 120° C.; alternatively, from about 0° C. to about 80° C.; alternatively, from about 10° C. to about 60° C.; alternatively, from about 10° C. to about 35° C.; or alternatively, from about 20° C. to about 40° C. In these and other aspects, these temperature ranges also are meant to encompass circumstances where the precontacting step and the formation of the precontacted mixture are conducted at a series of different temperatures, instead of at a single fixed temperature, falling within the respective ranges.

Similarly, the time required for the precontacting step and the formation of the precontacted mixture is not limited to any particular period of time (the first period of time). Whether a particular duration of the first period of time is suitable can depend upon, for example, the molar ratio of the alkylaluminum compound to the half-metallocene titanium compound, the temperature at which the components are contacted and the mixture is formed, the presence of diluents or solvents, and the degree of mixing, among other variables. Typically, however, a minimum first period of time can be about 1 minute, about 15 minutes, about 30 minutes, about 1 hour, or about 2 hours; additionally or alternatively, a maximum first period of time can be about 96 hours, about 48 hours, about 36 hours, about 30 hours, about 24 hours, about 18 hours, about 12 hours, about 6 hours, or about 4 hours. Generally, the first period of time can be in a range from any minimum time period disclosed herein to any maximum time period disclosed herein. Accordingly, suitable non-limiting ranges can include the following: from about 1 minute to about 96 hours, from about 15 minutes to about 48 hours, from about 30 minutes to about 36 hours, from about 1 hour to about 30 hours, or from about 2 hours to about 24 hours. Other suitable time periods are readily apparent from this disclosure.

Referring now to step (ii), in which the precontacted mixture can be contacted with an activator and an optional co-catalyst for a second period of time to form the catalyst composition. Step (ii), likewise, can be conducted at a variety of temperatures and time periods (a second period of time). For instance, step (ii) can be conducted at a temperature in a range from about 0° C. to about 120° C.; alternatively, from about 0° C. to about 80° C.; alternatively, from about 10° C. to about 60° C.; alternatively, from about 10° C. to about 35° C.; or alternatively, from about 20° C. to about 40° C. In these and other aspects, these temperature ranges also are meant to encompass circumstances where step (ii) is conducted at a series of different temperatures, instead of at a single fixed temperature, falling within the respective ranges. As an example, the precontacted mixture and the activator and co-catalyst (if used) can be contacted at an elevated temperature, following by cooling to a lower temperature for longer term storage of the finished catalyst composition.

The second period of time is not limited to any particular period of time. Hence, the second period of time can range from as little as 1-10 seconds to as long as 24-48 hours, or more. The appropriate second period of time can depend upon, for example, the temperature, the relative amounts of the precontacted mixture and the activator, the presence of diluents or solvents in step (ii), the degree of mixing, and considerations for long term storage, among other variables. Generally, however, the second period of time can be at least about 5 seconds, at least about 10 seconds, at least about 30 seconds, at least about 1 minute, at least about 5 minutes, at least about 10 minutes, and so forth. Assuming the catalyst composition is not intended for long term storage, which could extend for days or weeks, typical ranges for the second period of time can include, but are not limited to, from about 1 second to about 48 hours, from about 10 seconds to about 48 hours, from about 30 seconds to about 24 hours, from about 30 seconds to about 6 hours, from about 1 minute to about 6 hours, from about 5 minutes to about 24 hours, or from about 10 minutes to about 8 hours.

In an aspect of this invention, the activator in step (ii) can comprise an activator-support. For example, the activator-support can comprise a solid oxide treated with an electron-withdrawing anion. Alternatively, in another aspect, the activator-support can comprise a solid oxide treated with an electron-withdrawing anion, the solid oxide containing a Lewis-acidic metal ion. Non-limiting examples of suitable activator-supports are disclosed in, for instance, U.S. Pat. Nos. 7,294,599, 7,601,665, 7,884,163, 8,309,485, 8,623,973, 8,703,886, and 9,023,959, which are incorporated herein by reference in their entirety.

The solid oxide can encompass oxide materials such as alumina, “mixed oxides” thereof such as silica-alumina, coatings of one oxide on another, and combinations and mixtures thereof. The mixed oxides such as silica-alumina can be single or multiple chemical phases with more than one metal combined with oxygen to form the solid oxide. Examples of mixed oxides that can be used to form an activator-support, either singly or in combination, can include, but are not limited to, silica-alumina, silica-titania, silica-zirconia, alumina-titania, alumina-zirconia, zinc-aluminate, alumina-boria, silica-boria, aluminophosphate-silica, titania-zirconia, and the like. The solid oxide used herein also can encompass oxide materials such as silica-coated alumina, as described in U.S. Pat. No. 7,884,163 (e.g., Sasol Siral® 28, Sasol Siral® 40, etc.).

Accordingly, in one aspect, the solid oxide can comprise silica, alumina, silica-alumina, silica-coated alumina, aluminum phosphate, aluminophosphate, heteropolytungstate, titania, zirconia, magnesia, boria, zinc oxide, any mixed oxide thereof, or any combination thereof. In another aspect, the solid oxide can comprise alumina, silica-alumina, silica-coated alumina, aluminum phosphate, aluminophosphate, heteropolytungstate, titania, zirconia, magnesia, boria, or zinc oxide, as well as any mixed oxide thereof, or any mixture thereof. In another aspect, the solid oxide can comprise silica, alumina, titania, zirconia, magnesia, boria, zinc oxide, any mixed oxide thereof, or any combination thereof. In yet another aspect, the solid oxide can comprise silica-alumina, silica-coated alumina, silica-titania, silica-zirconia, alumina-boria, or any combination thereof. In still another aspect, the solid oxide can comprise alumina, silica-alumina, silica-coated alumina, or any mixture thereof; alternatively, alumina; alternatively, silica-alumina; or alternatively, silica-coated alumina.

The silica-alumina or silica-coated alumina solid oxide materials which can be used can have an silica content from about 5 to about 95% by weight. In one aspect, the silica content of these solid oxides can be from about 10 to about 80%, or from about 20% to about 70%, silica by weight. In another aspect, such materials can have silica contents ranging from about 15% to about 60%, from about 20% to about 50%, or from about 25% to about 45%, silica by weight. The solid oxides contemplated herein can have any suitable surface area, pore volume, and particle size, as would be recognized by those of skill in the art.

The electron-withdrawing component used to treat the solid oxide can be any component that increases the Lewis or Brønsted acidity of the solid oxide upon treatment (as compared to the solid oxide that is not treated with at least one electron-withdrawing anion). According to one aspect, the electron-withdrawing component can be an electron-withdrawing anion derived from a salt, an acid, or other compound, such as a volatile organic compound, that serves as a source or precursor for that anion. Examples of electron-withdrawing anions can include, but are not limited to, sulfate, bisulfate, fluoride, chloride, bromide, iodide, fluorosulfate, fluoroborate, phosphate, fluorophosphate, trifluoroacetate, triflate, fluorozirconate, fluorotitanate, phospho-tungstate, tungstate, molybdate, and the like, including mixtures and combinations thereof. In addition, other ionic or non-ionic compounds that serve as sources for these electron-withdrawing anions also can be employed. It is contemplated that the electron-withdrawing anion can be, or can comprise, fluoride, chloride, bromide, phosphate, triflate, bisulfate, or sulfate, and the like, or any combination thereof, in some aspects provided herein. In other aspects, the electron-withdrawing anion can comprise sulfate, bisulfate, fluoride, chloride, bromide, iodide, fluorosulfate, fluoroborate, phosphate, fluorophosphate, trifluoroacetate, triflate, fluorozirconate, fluorotitanate, and the like, or combinations thereof. Yet, in other aspects, the electron-withdrawing anion can comprise fluoride and/or sulfate.

The activator-support generally can contain from about 1 to about 25 wt. % of the electron-withdrawing anion, based on the weight of the activator-support. In particular aspects provided herein, the activator-support can contain from about 1 to about 20 wt. %, from about 2 to about 20 wt. %, from about 3 to about 20 wt. %, from about 2 to about 15 wt. %, from about 3 to about 15 wt. %, from about 3 to about 12 wt. %, or from about 4 to about 10 wt. %, of the electron-withdrawing anion, based on the total weight of the activator-support.

In an aspect, the activator-support can comprise fluorided alumina, chlorided alumina, bromided alumina, sulfated alumina, fluorided silica-alumina, chlorided silica-alumina, bromided silica-alumina, sulfated silica-alumina, fluorided silica-zirconia, chlorided silica-zirconia, bromided silica-zirconia, sulfated silica-zirconia, fluorided silica-titania, fluorided-chlorided silica-coated alumina, fluorided silica-coated alumina, sulfated silica-coated alumina, phosphated silica-coated alumina, and the like, as well as any mixture or combination thereof. In another aspect, the activator-support can be, or can comprise, a fluorided solid oxide and/or a sulfated solid oxide, non-limiting examples of which can include fluorided alumina, sulfated alumina, fluorided silica-alumina, sulfated silica-alumina, fluorided-chlorided silica-coated alumina, fluorided silica-coated alumina, sulfated silica-coated alumina, and the like, as well as combinations thereof. In yet another aspect, the activator-support can comprise fluorided alumina; alternatively, chlorided alumina; alternatively, sulfated alumina; alternatively, fluorided silica-alumina; alternatively, sulfated silica-alumina; alternatively, fluorided silica-zirconia; alternatively, chlorided silica-zirconia; alternatively, sulfated silica-coated alumina; alternatively, fluorided-chlorided silica-coated alumina; or alternatively, fluorided silica-coated alumina.

Various processes can be used to form activator-supports useful in the present invention. Methods of contacting the solid oxide with the electron-withdrawing component, suitable electron withdrawing components and addition amounts, impregnation with metals or metal ions (e.g., zinc, nickel, vanadium, titanium, silver, copper, gallium, tin, tungsten, molybdenum, zirconium, and the like, or combinations thereof), and various calcining procedures and conditions are disclosed in, for example, U.S. Pat. Nos. 6,107,230, 6,165,929, 6,294,494, 6,300,271, 6,316,553, 6,355,594, 6,376,415, 6,388,017, 6,391,816, 6,395,666, 6,524,987, 6,548,441, 6,548,442, 6,576,583, 6,613,712, 6,632,894, 6,667,274, 6,750,302, 7,294,599, 7,601,665, 7,884,163, and 8,309,485, which are incorporated herein by reference in their entirety. Other suitable processes and procedures for preparing activator-supports (e.g., fluorided or sulfated solid oxides) are well known to those of skill in the art.

In a further aspect, the catalyst composition of step (ii) can be substantially free of aluminoxanes, organoboron or organoborate compounds, ionizing ionic compounds, or combinations thereof; alternatively, substantially free of aluminoxanes; alternatively, substantially free or organoboron or organoborate compounds; or alternatively, substantially free of ionizing ionic compounds. In these aspects, the catalyst composition has suitable catalyst activity in the absence of these additional materials. For example, a catalyst composition comprising a half-metallocene titanium phosphinimide compound, an activator-support, and an alkylaluminum compound can include no other materials that would increase/decrease the activity of the catalyst composition by more than about 10% from the catalyst activity of the catalyst composition in the absence of said materials.

However, in other aspects of this invention, these activators can be employed in step (ii). Thus, the activator in step (ii) can comprise an aluminoxane compound (e.g., a supported aluminoxane), an organoboron or organoborate compound, an ionizing ionic compound, or combinations thereof alternatively, an aluminoxane compound; alternatively, an organoboron or organoborate compound; or alternatively, an ionizing ionic compound.

Consistent with particular aspects of this invention, step (ii) can comprise contacting the precontacted mixture with the activator and the co-catalyst, and any suitable co-catalyst can be used. In one aspect, the co-catalyst can be an organoaluminum compound, representative examples of which can include trimethylaluminum, triethylaluminum, tri-n-propylaluminum, tri-n-butylaluminum, triisobutylaluminum, tri-n-hexylaluminum, tri-n-octylaluminum, diisobutylaluminum hydride, diethylaluminum ethoxide, diethylaluminum chloride, and the like, or combinations thereof. Thus, the organoaluminum co-catalyst in step (ii) can be the same as or different from the alkylaluminum compound in step (i). In another aspect, when the activator comprises an activator-support, the co-catalyst can comprise an aluminoxane compound, an organoboron or organoborate compound, an ionizing ionic compound, an organoaluminum compound, an organozinc compound, an organomagnesium compound, an organolithium compound, and the like, or any combination thereof or alternatively, an organoaluminum compound, an organozinc compound, an organomagnesium compound, an organolithium compound, or any combination thereof. More than one co-catalyst can be present in the catalyst composition, although a co-catalyst is not required in step (ii). Additional information on co-catalysts can be found in, for example, U.S. Pat. Nos. 3,242,099, 4,794,096, 4,808,561, 5,576,259, 5,807,938, 5,919,983, 7,294,599 7,601,665, 7,884,163, 8,114,946, and 8,309,485, which are incorporated herein by reference in their entirety.

Generally, the weight ratio of alkylaluminum compound and co-catalyst (if used) to activator (e.g., activator-support) can be in a range from about 10:1 to about 1:1000. If more than one co-catalyst compound and/or more than one activator are employed, this ratio is based on the total weight of each respective component. In another aspect, the weight ratio can be in a range from about 3:1 to about 1:500, or from about 1:10 to about 1:350.

In some aspects of this invention, the weight ratio of the half-metallocene titanium phosphinimide compound to the activator (e.g., activator-support) can be in a range from about 1:1 to about 1:1,000,000. If more than one titanium compound and/or more than activator is/are employed, this ratio is based on the total weights of the respective components. In another aspect, this weight ratio can be in a range from about 1:5 to about 1:100,000, or from about 1:10 to about 1:10,000. Yet, in another aspect, the weight ratio of the titanium compound to the activator can be in a range from about 1:20 to about 1:1000.

Catalyst compositions of the present invention generally have a catalyst activity greater than about 20,000 grams, greater than about 50,000 grams, greater than about 70,000 grams, greater than about 100,000 grams, etc., of ethylene polymer (homopolymer or copolymer, as the context requires) per gram of the half-metallocene titanium phosphinimide compound per hour (abbreviated g/g/h). In another aspect, the catalyst activity can be greater than about 150,000, greater than about 200,000, or greater than about 300,000 g/g/h, and often can range up to 400,000-750,000 g/g/h. These activities are measured under slurry polymerization conditions, with triisobutylaluminum as the alkylaluminum compound, using isobutane as the diluent, at a polymerization temperature of 80° C. and a reactor pressure of 340 psig. Additionally, in some aspects, the activator can comprise an activator-support, such as sulfated alumina, fluorided-chlorided silica-coated alumina, or fluorided silica-coated alumina, although not limited thereto. Generally, the precontacting step does not significantly changes the activity of the resultant catalyst composition.

Referring now to step (iii), in which the catalyst composition can be contacted with an olefin monomer and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce an olefin polymer. The olefin polymerization process can use any suitable types of polymerization reactor systems and reactors. The polymerization reactor system can include any polymerization reactor capable of polymerizing olefin monomers and comonomers (one or more than one comonomer) to produce homopolymers, copolymers, terpolymers, and the like. The various types of reactors include those that can be referred to as a loop reactor, slurry reactor, gas-phase reactor, solution reactor, high pressure reactor, tubular reactor, autoclave reactor, and the like, or combinations thereof. Suitable polymerization conditions are used for the various reactor types. Gas phase reactors can comprise fluidized bed reactors or staged horizontal reactors. Slurry reactors can comprise vertical or horizontal loops. High pressure reactors can comprise autoclave or tubular reactors. Reactor types can include batch or continuous processes. Continuous processes can use intermittent or continuous product discharge. Processes can also include partial or full direct recycle of unreacted monomer, unreacted comonomer, and/or diluent.

Polymerization reactor systems of the present invention can comprise one type of reactor in a system or multiple reactors of the same or different type (e.g., a single reactor, dual reactor, more than two reactors). Production of polymers in multiple reactors can include several stages in at least two separate polymerization reactors interconnected by a transfer device making it possible to transfer the polymers resulting from the first polymerization reactor into the second reactor. The desired polymerization conditions in one of the reactors can be different from the operating conditions of the other reactor(s). Alternatively, polymerization in multiple reactors can include the manual transfer of polymer from one reactor to subsequent reactors for continued polymerization. Multiple reactor systems can include any combination including, but not limited to, multiple loop reactors, multiple gas phase reactors, a combination of loop and gas phase reactors, multiple high pressure reactors, or a combination of high pressure with loop and/or gas phase reactors. The multiple reactors can be operated in series, in parallel, or both. Accordingly, the present invention encompasses polymerization reactor systems comprising a single reactor, comprising two reactors, and comprising more than two reactors. The polymerization reactor system can comprise a slurry reactor (e.g., a loop slurry reactor), a gas-phase reactor, a solution reactor, in certain aspects of this invention, as well as multi-reactor combinations thereof.

According to one aspect of the invention, the polymerization reactor system can comprise at least one loop slurry reactor comprising vertical or horizontal loops. Monomer, diluent, catalyst, and comonomer can be continuously fed to a loop reactor where polymerization occurs. Generally, continuous processes can comprise the continuous introduction of monomer/comonomer, a catalyst, and a diluent into a polymerization reactor and the continuous removal from this reactor of a suspension comprising polymer particles and the diluent. Reactor effluent can be flashed to remove the solid polymer from the liquids that comprise the diluent, monomer and/or comonomer. Various technologies can be used for this separation step including, but not limited to, flashing that can include any combination of heat addition and pressure reduction, separation by cyclonic action in either a cyclone or hydrocyclone, or separation by centrifugation.

A typical slurry polymerization process (also known as the particle form process) is disclosed, for example, in U.S. Pat. Nos. 3,248,179, 4,501,885, 5,565,175, 5,575,979, 6,239,235, 6,262,191, 6,833,415, and 8,822,608, each of which is incorporated herein by reference in its entirety.

Suitable diluents used in slurry polymerization include, but are not limited to, the monomer being polymerized and hydrocarbons that are liquids under polymerization conditions. Examples of suitable diluents include, but are not limited to, hydrocarbons such as propane, cyclohexane, isobutane, n-butane, n-pentane, isopentane, neopentane, and n-hexane. Some loop polymerization reactions can occur under bulk conditions where no diluent is used, such as can be employed in the bulk polymerization of propylene to form polypropylene homopolymers.

According to yet another aspect of this invention, the polymerization reactor system can comprise at least one gas phase reactor. Such systems can employ a continuous recycle stream containing one or more monomers continuously cycled through a fluidized bed in the presence of the catalyst under polymerization conditions. A recycle stream can be withdrawn from the fluidized bed and recycled back into the reactor. Simultaneously, polymer product can be withdrawn from the reactor and new or fresh monomer can be added to replace the polymerized monomer. Such gas phase reactors can comprise a process for multi-step gas-phase polymerization of olefins, in which olefins are polymerized in the gaseous phase in at least two independent gas-phase polymerization zones while feeding a catalyst-containing polymer formed in a first polymerization zone to a second polymerization zone. One type of gas phase reactor is disclosed in U.S. Pat. Nos. 5,352,749, 4,588,790, 5,436,304, 7,531,606, and 7,598,327, each of which is incorporated by reference in its entirety herein.

According to still another aspect of the invention, a high pressure polymerization reactor can comprise a tubular reactor or an autoclave reactor. Tubular reactors can have several zones where fresh monomer, initiators, or catalysts are added. Monomer can be entrained in an inert gaseous stream and introduced at one zone of the reactor. Initiators, catalysts, and/or catalyst components can be entrained in a gaseous stream and introduced at another zone of the reactor. The gas streams can be intermixed for polymerization. Heat and pressure can be employed appropriately to obtain optimal polymerization reaction conditions.

According to yet another aspect of the invention, the polymerization reactor system can comprise a solution polymerization reactor wherein the monomer (and comonomer, if used) are contacted with the catalyst composition by suitable stirring or other means. A carrier comprising an inert organic diluent or excess monomer can be employed. If desired, the monomer/comonomer can be brought in the vapor phase into contact with the catalytic reaction product, in the presence or absence of liquid material. The polymerization zone is maintained at temperatures and pressures that will result in the formation of a solution of the polymer in a reaction medium. Agitation can be employed to obtain better temperature control and to maintain uniform polymerization mixtures throughout the polymerization zone. Adequate means are utilized for dissipating the exothermic heat of polymerization.

Polymerization reactor systems suitable for the present invention can further comprise any combination of at least one raw material feed system, at least one feed system for catalyst or catalyst components, and/or at least one polymer recovery system. Suitable reactor systems for the present invention can further comprise systems for feedstock purification, catalyst storage and preparation, extrusion, reactor cooling, polymer recovery, fractionation, recycle, storage, loadout, laboratory analysis, and process control.

Polymerization conditions that are controlled for efficiency and to provide desired polymer properties can include temperature, pressure, and the concentrations of various reactants. Polymerization temperature can affect catalyst productivity, polymer molecular weight, and molecular weight distribution. A suitable polymerization temperature can be any temperature below the de-polymerization temperature according to the Gibbs Free energy equation. Typically, this includes from about 35° C. to about 280° C., for example, or from about 50° C. to about 175° C., depending upon the type of polymerization reactor(s). In some reactor systems, the polymerization temperature generally can fall within a range from about 60° C. to about 120° C., or from about 70° C. to about 100° C. Various polymerization conditions can be held substantially constant, for example, for the production of a particular grade of olefin polymer.

Suitable pressures will also vary according to the reactor and polymerization type. The pressure for liquid phase polymerizations in a loop reactor is typically less than 1000 psig (6.9 MPa). The pressure for gas phase polymerization is usually at about 200 to 500 psig (1.4 MPa to 3.4 MPa). High pressure polymerization in tubular or autoclave reactors is generally conducted at about 20,000 to 75,000 psig (138 to 517 MPa). Polymerization reactors can also be operated in a supercritical region occurring at generally higher temperatures and pressures (for instance, above 92° C. and 700 psig (4.83 MPa)). Operation above the critical point of a pressure/temperature diagram (supercritical phase) can offer advantages to the polymerization reaction process.

Aspects of this invention are directed to olefin polymerization processes conducted in the absence of added hydrogen. An olefin polymerization process of this invention can comprise contacting a catalyst composition with an olefin monomer and optionally an olefin comonomer in a polymerization reactor system under polymerization conditions to produce an olefin polymer, wherein the catalyst composition is produced as disclosed in steps (i) and (ii), and wherein the polymerization process is conducted in the absence of added hydrogen (no hydrogen is added to the polymerization reactor system). As one of ordinary skill in the art would recognize, hydrogen can be generated in-situ by catalyst compositions in various olefin polymerization processes, and the amount generated can vary depending upon the specific catalyst composition and metallocene compound employed, the type of polymerization process used, the polymerization reaction conditions utilized, and so forth.

In other aspects, it may be desirable to conduct the polymerization process in the presence of a certain amount of added hydrogen. Accordingly, an olefin polymerization process of this invention can comprise contacting a catalyst composition with an olefin monomer and optionally an olefin comonomer in a polymerization reactor system under polymerization conditions to produce an olefin polymer, wherein the catalyst composition is produced as disclosed in steps (i) and (ii), and wherein the polymerization process is conducted in the presence of added hydrogen (hydrogen is added to the polymerization reactor system). For example, the ratio of hydrogen to the olefin monomer in the polymerization process can be controlled, often by the feed ratio of hydrogen to the olefin monomer entering the reactor. The added hydrogen to olefin monomer ratio in the process can be controlled at a weight ratio which falls within a range from about 25 ppm to about 1500 ppm, from about 50 to about 1000 ppm, or from about 100 ppm to about 750 ppm.

In some aspects of this invention, the feed or reactant ratio of hydrogen to olefin monomer can be maintained substantially constant during the polymerization run for a particular polymer grade. That is, the hydrogen:olefin monomer ratio can be selected at a particular ratio within a range from about 5 ppm up to about 1000 ppm or so, and maintained at the ratio to within about +/−25% during the polymerization run. For instance, if the target ratio is 100 ppm, then maintaining the hydrogen:olefin monomer ratio substantially constant would entail maintaining the feed ratio between about 75 ppm and about 125 ppm. Further, the addition of comonomer (or comonomers) can be, and generally is, substantially constant throughout the polymerization run for a particular polymer grade.

However, in other aspects, it is contemplated that monomer, comonomer (or comonomers), and/or hydrogen can be periodically pulsed to the reactor, for instance, in a manner similar to that employed in U.S. Pat. No. 5,739,220 and U.S. Patent Publication No. 2004/0059070, the disclosures of which are incorporated herein by reference in their entirety.

The concentration of the reactants entering the polymerization reactor system can be controlled to produce resins with certain physical and mechanical properties. The proposed end-use product that will be formed by the polymer resin and the method of forming that product ultimately can determine the desired polymer properties and attributes. Mechanical properties include tensile, flexural, impact, creep, stress relaxation, and hardness tests. Physical properties include density, molecular weight, molecular weight distribution, melting temperature, glass transition temperature, temperature melt of crystallization, density, stereoregularity, crack growth, long chain branching, and rheological measurements.

This invention also is directed to, and encompasses, the polymers (e.g., ethylene/α-olefin copolymers, ethylene homopolymers, etc.) produced by any of the polymerization processes disclosed herein. Articles of manufacture can be formed from, and/or can comprise, the polymers produced in accordance with this invention.

Olefin Monomers and Polymers

Olefin monomers contemplated herein typically include olefin compounds having from 2 to 30 carbon atoms per molecule and having at least one olefinic double bond. Homopolymerization processes using a single olefin, such as ethylene, propylene, butene, hexene, octene, and the like, are encompassed, as well as copolymerization and terpolymerization reactions using an olefin monomer with at least one different olefinic compound.

As an example, any resultant ethylene copolymers and terpolymers generally can contain a major amount of ethylene (>50 mole percent) and a minor amount of comonomer (<50 mole percent). Comonomers that can be copolymerized with ethylene often have from 3 to 20 carbon atoms in their molecular chain.

Acyclic, cyclic, polycyclic, terminal (a), internal, linear, branched, substituted, unsubstituted, functionalized, and non-functionalized olefins can be employed. For example, typical unsaturated compounds that can be polymerized to produce olefin polymers can include, but are not limited to, ethylene, propylene, 1-butene, 2-butene, 3-methyl-1-butene, isobutylene, 1-pentene, 2-pentene, 3-methyl-1-pentene, 4-methyl-1-pentene, 1-hexene, 2-hexene, 3-hexene, 3-ethyl-1-hexene, 1-heptene, 2-heptene, 3-heptene, the four normal octenes (e.g., 1-octene), the four normal nonenes, the five normal decenes, and the like, or mixtures of two or more of these compounds. Cyclic and bicyclic olefins, including but not limited to, cyclopentene, cyclohexene, norbornylene, norbornadiene, and the like, also can be polymerized as described herein. Styrene also can be employed as a monomer or as a comonomer. In an aspect, the olefin monomer can comprise a C₂-C₂₀ olefin; alternatively, a C₂-C₁₂ olefin; alternatively, a C₆-C₂₄ olefin; alternatively, a C₂-C₁₀ α-olefin; alternatively, propylene, 1-butene, 1-pentene, 1-hexene, 1-heptene, 1-octene, 1-decene, or styrene; alternatively, ethylene, propylene, 1-butene, 1-hexene, or 1-octene; alternatively, ethylene or propylene; alternatively, ethylene; or alternatively, propylene.

When a copolymer (or alternatively, a terpolymer) is desired, the olefin monomer can comprise, for example, ethylene or propylene, which is copolymerized with at least one comonomer. According to one aspect, the olefin monomer in the polymerization process can comprise ethylene. In this aspect, examples of suitable olefin comonomers can include, but are not limited to, propylene, 1-butene, 2-butene, 3-methyl-1-butene, isobutylene, 1-pentene, 2-pentene, 3-methyl-1-pentene, 4-methyl-1-pentene, 1-hexene, 2-hexene, 3-ethyl-1-hexene, 1-heptene, 2-heptene, 3-heptene, 1-octene, 1-decene, styrene, and the like, or combinations thereof. According to another aspect, the olefin monomer can comprise ethylene and the olefin comonomer can comprise a C₃-C₁₀ α-olefin, while in yet another aspect, the comonomer can comprise propylene, 1-butene, 1-pentene, 1-hexene, 1-octene, 1-decene, styrene, or any combination thereof or alternatively, the olefin comonomer can comprise 1-butene, 1-hexene, 1-octene, or a combination thereof.

Generally, the amount of comonomer introduced into a polymerization reactor to produce the copolymer can be from about 0.01 weight percent to about 50 weight percent of the comonomer based on the total weight of the monomer and comonomer. According to another aspect, the amount of comonomer introduced into a polymerization reactor can be from about 0.01 weight percent to about 40 weight percent comonomer based on the total weight of the monomer and comonomer. In still another aspect, the amount of comonomer introduced into a polymerization reactor can be from about 0.1 weight percent to about 35 weight percent comonomer based on the total weight of the monomer and comonomer. Yet, in another aspect, the amount of comonomer introduced into a polymerization reactor can be from about 0.5 weight percent to about 20 weight percent comonomer based on the total weight of the monomer and comonomer.

While not intending to be bound by this theory, where branched, substituted, or functionalized olefins are used as reactants, it is believed that a steric hindrance can impede and/or slow the polymerization reaction. Thus, branched and/or cyclic portion(s) of the olefin removed somewhat from the carbon-carbon double bond would not be expected to hinder the reaction in the way that the same olefin substituents situated more proximate to the carbon-carbon double bond might.

According to one aspect, at least one monomer/reactant can be ethylene, so the polymerization reaction can be a homopolymerization involving only ethylene, or a copolymerization with a different acyclic, cyclic, terminal, internal, linear, branched, substituted, or unsubstituted olefin. In addition, the methods disclosed herein intend for olefin to also encompass diolefin compounds that include, but are not limited to, 1,3-butadiene, isoprene, 1,4-pentadiene, 1,5-hexadiene, and the like.

Olefin polymers encompassed herein can include any polymer produced from any olefin monomer (and optional comonomer(s)) described herein. For example, the olefin polymer can comprise an ethylene homopolymer, a propylene homopolymer, an ethylene copolymer (e.g., ethylene/1-butene, ethylene/1-hexene, or ethylene/1-octene), a propylene random copolymer, a propylene block copolymer, and the like, including combinations thereof. In one aspect, the olefin polymer can comprise an ethylene homopolymer, an ethylene/1-butene copolymer, an ethylene/1-hexene copolymer, and/or an ethylene/1-octene copolymer, while in another aspect, the olefin polymer can comprise an ethylene/1-hexene copolymer.

If the resultant polymer produced in accordance with the present invention is, for example, an ethylene polymer, its properties can be characterized by various analytical techniques known and used in the polyolefin industry. Articles of manufacture can be formed from, and/or can comprise, the ethylene polymers of this invention, whose typical properties are provided below.

The densities of ethylene polymers produced using the catalyst systems and polymerization processes described herein often range from about 0.87 to about 0.96 g/cm³. In one aspect of this invention, the density of the ethylene polymer can be in a range from about 0.93 to about 0.96, or from about 0.87 to about 0.94 g/cm³. Yet, in another aspect, the density can be in a range from about 0.88 to about 0.93 g/cm³, such as, for example, from about 0.89 to about 0.93 g/cm³, from about 0.895 to about 0.925 g/cm³, or from about 0.90 to about 0.92 g/cm³.

Suitable non-limiting ranges for the high load melt index (HLMI) of the ethylene polymer can include a HLMI less than or equal to about 200, less than or equal to about 100, less than or equal to about 50, or less than or equal to about 25 g/10 min. In some aspects, the ethylene polymer can have a HLMI in a range from about 1 to about 200, from about 1 to about 100, from about 1 to about 50, from about 5 to about 50, or from about 5 to about 25 g/10 min.

The ethylene polymer, in some aspects, can have a relatively broad molecular weight distribution, with a ratio of Mw/Mn in a range from about 2 to about 18, for example, from about 2.5 to about 15, from about 3 to about 15, or from about 3 to about 12. Generally, the ethylene polymer can have a number-average molecular weight (Mn) in a range from about 10,000 to about 150,000, from about 10,000 to about 100,000, from about 12,000 to about 100,000, or from about 14,000 to about 90,000 g/mol. Additionally or alternatively, the ethylene polymer can have a weight-average molecular weight (Mw) in a range from about 50,000 to about 750,000, from about 60,000 to about 600,000, from about 70,000 to about 500,000, or from about 100,000 to about 500,000 g/mol. Other suitable ranges for Mw can include, but are not limited to, from about 100,000 to about 750,000, from about 140,000 to about 500,000, or from about 150,000 to about to about 450,000 g/mol.

The ethylene polymer, in some aspects, can have ratio of Mz/Mw in a range from about 1.8 to about 10, for example, from about 2 to about 10, from about 2 to about 9, or from about 2 to about 8. Generally, the ethylene polymer can have a z-average molecular weight (Mz) in a range from about 300,000 to about 2,500,000, from about 300,000 to about 1,500,000, from about 500,000 to about 1,500,000, or from about 500,000 to about 1,000,000 g/mol. Other suitable ranges for Mz can include, but are not limited to, from about 600,000 to about 1,250,000, from about 750,000 to about 1,000,000, or from about 1,000,000 to about 1,500,000 g/mol. Additionally or alternatively, the ethylene polymer can have a peak molecular weight (Mp) in a range from about 50,000 to about 500,000, from about 60,000 to about 400,000, from about 50,000 to about 250,000, from about 100,000 to about 250,000, or from about 200,000 to about 500,000 g/mol. In these and other aspects, the ethylene polymer can have a unimodal molecular weight distribution.

Polymers of ethylene, whether homopolymers, copolymers, and so forth, can be formed into various articles of manufacture. Articles which can comprise polymers of this invention include, but are not limited to, an agricultural film, an automobile part, a bottle, a drum, a fiber or fabric, a food packaging film or container, a food service article, a fuel tank, a geomembrane, a household container, a liner, a molded product, a medical device or material, a pipe, a sheet or tape, a toy, and the like. Various processes can be employed to form these articles. Non-limiting examples of these processes include injection molding, blow molding, rotational molding, film extrusion, sheet extrusion, profile extrusion, thermoforming, and the like. Additionally, additives and modifiers often are added to these polymers in order to provide beneficial polymer processing or end-use product attributes. Such processes and materials are described in Modern Plastics Encyclopedia, Mid-November 1995 Issue, Vol. 72, No. 12; and Film Extrusion Manual—Process, Materials, Properties, TAPPI Press, 1992; the disclosures of which are incorporated herein by reference in their entirety.

Also contemplated herein is a method for forming or preparing an article of manufacture that comprises a polymer produced by any of the polymerization processes disclosed herein. For instance, the method can comprise (I) contacting a catalyst composition with an olefin monomer and an optional olefin comonomer under polymerization conditions in a polymerization reactor system to produce an olefin polymer, wherein the catalyst composition is produced as disclosed in steps (i) and (ii); and (II) forming an article of manufacture comprising the olefin polymer. The forming step can comprise blending, melt processing, extruding, molding, or thermoforming, and the like, including combinations thereof.

Processes Relating to Molecular Weight Distribution

Consistent with an aspect of this invention, a process for controlling the molecular weight distribution (i.e., the ratio of Mw/Mn) of an ethylene polymer can comprise (A) contacting a catalyst composition with ethylene and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce the ethylene polymer, wherein the catalyst composition can comprise a half-metallocene titanium phosphinimide compound, an activator, and an alkylaluminum compound, and (B) adjusting a solubility parameter of the alkylaluminum compound to control the ratio of Mw/Mn of the ethylene polymer. Consistent with another aspect of this invention, a process for producing an ethylene polymer with a target ratio of Mw/Mn can comprise (a) selecting an alkylaluminum compound based on a solubility parameter of the alkylaluminum compound, and (b) contacting a catalyst composition with ethylene and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce the ethylene polymer with the target ratio of Mw/Mn. The catalyst composition can comprise a half-metallocene titanium phosphinimide compound, an activator, and the alkylaluminum compound. Thus, in these processes, the alkylaluminum compound can be used to control the molecular weight distribution (the ratio of Mw/Mn) of the polymer produced.

Generally, the features of these processes (e.g., the activator, the alkylaluminum compound, the half-metallocene compound, the olefin comonomer, and the Mw/Mn of the ethylene polymer, among others) are independently described herein, and these features can be combined in any combination to further describe the disclosed processes. Moreover, other process steps can be conducted before, during, and/or after any of the steps listed in the disclosed processes, unless stated otherwise. Additionally, ethylene polymers produced in accordance with the disclosed processes are within the scope of this disclosure and are encompassed herein.

In these processes for controlling the ratio of Mw/Mn of the ethylene polymer and for producing the ethylene polymer with the target ratio of Mw/Mn, the selections for the half-metallocene titanium phosphinimide compound, the activator, and the alkylaluminum compound (and thus, the catalyst composition) can be the same as those described herein for the olefin polymerization process. Therefore, the half-metallocene titanium phosphinimide compound can have formula (B), and can have any suitable selections for Cp, R¹, R², R³, X¹, and X². For instance, Cp can be a substituted or unsubstituted cyclopentadienyl or indenyl group, while R¹, R², and R³ independently can be H or a C₁ to C₁₈ hydrocarbyl group, and X¹ and X² can be a halide (e.g., Cl). Likewise, the activator can comprise an activator-support, an aluminoxane compound, an organoboron or organoborate compound, an ionizing ionic compound, or any combination thereof.

Similarly, the selections for the polymerization reactor system (e.g., a slurry reactor, a gas-phase reactor, a solution reactor, or any combination thereof), polymerization conditions (e.g., temperature, pressure, and use of hydrogen), olefin comonomer (e.g., 1-butene, 1-hexene, 1-octene, or a mixture thereof), and ethylene polymer (e.g., ethylene homopolymer, ethylene/1-butene copolymer, ethylene/1-hexene copolymer, and/or ethylene/1-octene copolymer, and associated polymer properties) can be the same as those described herein for the olefin polymerization process.

Referring now to the process for controlling a ratio of Mw/Mn of an ethylene polymer, this process can comprise (A) contacting a catalyst composition with ethylene and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce the ethylene polymer, wherein the catalyst composition comprises a half-metallocene titanium phosphinimide compound, an activator, and an alkylaluminum compound, and (B) adjusting a solubility parameter of the alkylaluminum compound to control the ratio of Mw/Mn of the ethylene polymer. Unexpectedly, it was found that the Mw/Mn of the ethylene polymer generally increases as the solubility parameter of the alkylaluminum compound decreases. Thus, in this process, adjusting the solubility parameter of the alkylaluminum compound can be used to control the ratio of Mw/Mn of the ethylene polymer produced in the process. For instance, if the ratio of Mw/Mn needs to be increased, the solubility parameter of the alkylaluminum compound used in the catalyst system can be decreased by utilizing an alkylaluminum compound with a lower solubility parameter, or by utilizing a mixture of two alkylaluminum compounds resulting in lower solubility parameter for the mixture of the alkylaluminum compounds.

In one aspect, the ratio of Mw/Mn of the ethylene polymer is less than or equal to about 6, and the alkylaluminum compound can comprise trimethylaluminum, triethylaluminum, or a combination thereof. In this aspect, the ethylene polymer typically can have a ratio of Mw/Mn in a range from about 2.5 to about 6, from about 2.5 to about 5.5, from about 3 to about 6, or from about 3 to about 5.5.

In another aspect, the ratio of Mw/Mn of the ethylene polymer is greater than or equal to about 6, and the alkylaluminum compound can comprise triisobutylaluminum, trioctylaluminum, or a combination thereof. In this aspect, the ethylene polymer typically can have a ratio of Mw/Mn in a from about 6 to about 18, from about 6.5 to about 15, or from about 7 to about 17.

Referring now to the process for producing an ethylene polymer with a target ratio of Mw/Mn, this process can comprise (a) selecting an alkylaluminum compound based on a solubility parameter of the alkylaluminum compound, and (b) contacting a catalyst composition with ethylene and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce the ethylene polymer with the target ratio of Mw/Mn. The catalyst composition can comprise a half-metallocene titanium phosphinimide compound, an activator, and the alkylaluminum compound. As above, it was found, unexpectedly, that the Mw/Mn of the ethylene polymer generally increases as the solubility parameter of the alkylaluminum compound decreases. Thus, in this process, a particular alkylaluminum compound (or combination of two or more alkylaluminum compounds) can be selected for use in the catalyst composition based on the solubility parameter of the alkylaluminum compound(s) and the desired or target ratio of Mw/Mn of the ethylene polymer.

For instance, if a ratio of Mw/Mn of less than or equal to about 6 is desired or targeted, the alkylaluminum compound often comprises trimethylaluminum, triethylaluminum, or a combination thereof. In such circumstances, the ethylene polymer produced by the process can have a ratio of Mw/Mn in a range from about 2.5 to about 6, from about 2.5 to about 5.5, from about 3 to about 6, or from about 3 to about 5.5.

In contrast, if a ratio of Mw/Mn of greater than or equal to about 6 is desired or targeted, the alkylaluminum compound often comprises triisobutylaluminum, trioctylaluminum, or a combination thereof. In such circumstances, the ethylene polymer produced by the process can have a ratio of Mw/Mn in a range from about 6 to about 18, from about 6.5 to about 15, or from about 7 to about 17.

EXAMPLES

The invention is further illustrated by the following examples, which are not to be construed in any way as imposing limitations to the scope of this invention. Various other aspects, modifications, and equivalents thereof which, after reading the description herein, can suggest themselves to one of ordinary skill in the art without departing from the spirit of the present invention or the scope of the appended claims.

Melt index (MI, g/10 min) was determined in accordance with ASTM D1238 at 190° C. with a 2,160 gram weight, and high load melt index (HLMI, g/10 min) was determined in accordance with ASTM D1238 at 190° C. with a 21,600 gram weight.

Molecular weights and molecular weight distributions were obtained using a PL-GPC 220 (Polymer Labs, an Agilent Company) system equipped with a IR4 detector (Polymer Char, Spain) and three Styragel HMW-6E GPC columns (Waters, Mass.) running at 145° C. The flow rate of the mobile phase 1,2,4-trichlorobenzene (TCB) containing 0.5 g/L 2,6-di-t-butyl-4-methylphenol (BHT) was set at 1 mL/min, and polymer solution concentrations were in the range of 1.0-1.5 mg/mL, depending on the molecular weight. Sample preparation was conducted at 150° C. for nominally 4 hr with occasional and gentle agitation, before the solutions were transferred to sample vials for injection. An injection volume of about 200 μL was used. The integral calibration method was used to deduce molecular weights and molecular weight distributions using a Chevron Phillips Chemical Company's HDPE polyethylene resin, MARLEX® BHB5003, as the standard. The integral table of the standard was pre-determined in a separate experiment with SEC-MALS. Mn is the number-average molecular weight, Mw is the weight-average molecular weight, and Mz is the z-average molecular weight.

Fluorided silica-coated alumina activator-supports were prepared as follows. Bohemite was obtained from W.R. Grace & Company under the designation “Alumina A” and having a surface area of 300 m²/g, a pore volume of 1.3 mL/g, and an average particle size of 100 microns. The alumina was first calcined in dry air at about 600° C. for approximately 6 hours, cooled to ambient temperature, and then contacted with tetraethylorthosilicate in isopropanol to equal 25 wt. % SiO₂. After drying, the silica-coated alumina was calcined at 600° C. for 3 hours. Fluorided silica-coated alumina (7 wt. % F) was prepared by impregnating the calcined silica-coated alumina with an ammonium bifluoride solution in methanol, drying, and then calcining for 3 hours at 600° C. in dry air. Afterward, the fluorided silica-coated alumina (FSCA) was collected and stored under dry nitrogen, and was used without exposure to the atmosphere.

Examples 1-17

The general procedure for the polymerization experiments was performed as follows, either with or without a pre-contacting step during catalyst preparation. The polymerization experiments were conducted in a one-gallon stainless steel reactor, and isobutane (1.2 L) was used in all experiments. Solutions of the half-metallocene titanium phosphinimide compound were prepared at about 1 mg/mL in toluene. In experiments where a pre-contacting step was employed, the half-metallocene titanium phosphinimide solution was combined with an alkylaluminum solution (1 M in hexanes) at a 1:1-5:1 molar ratio of Al:Ti for 16-24 hours at room temperature to form the precontacted mixture.

The activator-support (FSCA) or borane (tris(pentafluorophenyl)boron; 1:1 molar ratio of B:Ti), an additional amount of an organoaluminum compound (same compound used in the pre-contacting step; 150 ppm by weight of the organoaluminum compound based on the weight of isobutane), and either the precontacted mixture (formed from combining the half-metallocene titanium phosphinimide solution and the alkylaluminum solution) or the solution of the half-metallocene titanium phosphinimide were added in that order through a charge port while slowly venting isobutane vapor. An exception was Example 11, where the FSCA, alkylaluminum, and the titanium half-metallocene titanium solution were contacted in that order to form the catalyst system. The charge port was closed and isobutane was added. The contents of the reactor were stirred and heated to the desired polymerization temperature of 80° C. Ethylene, 1-hexene (10 grams), and hydrogen (ranging from 125 to 250 ppm by weight, based on ethylene) were then introduced into the reactor. Ethylene and hydrogen were fed on demand to maintain the target pressure of 340 psig for 20 minutes (Examples 9 and 10 were conducted for 30 and 60 minutes, respectively). The reactor was maintained at 80° C. throughout the run by an automated heating-cooling system. After venting of the reactor, purging, and cooling, the resulting polymer product was dried under reduced pressure.

The structures of half-metallocene titanium phosphinimide compounds MET-1 and MET-2 are shown below (MET-3 was similar to MET-2, but with a pentamethyl-cyclopentadienyl group):

As shown in Table I, different activators (FSCA or borane), alkylaluminum compounds (TIBA=triisobutylaluminum, TEA=triethylaluminum, TMA=trimethylaluminum, and TOA=trioctylaluminum), and half-metallocene titanium compounds were employed in polymerization experiments, performed as described above, either with a pre-contacting step during catalyst preparation, or where all catalyst components were combined substantially contemporaneously. The catalyst activity in Table I is listed in grams of polymer per gram of titanium half-metallocene phosphinimide compound per hour. Unexpectedly, the use of DEAC (diethylaluminum chloride) in Example 7 resulted in a catalyst system with no polymerization activity.

Table II summarizes certain polymer properties for the polymers produced in Examples 1-17, FIGS. 1-8 illustrate the molecular weight distributions (amount of polymer versus the logarithm of molecular weight) for the some of the polymers shown in Table II, and FIG. 9 is a bar chart that demonstrates the impact of the pre-contacting step on the Mw.

Unexpectedly, these tables and figures demonstrate that ethylene polymers produced using the catalyst compositions prepared using a pre-contacting step generally had much higher molecular weights (Mw) than the ethylene polymer produced using the same catalyst system without the pre-contacting step (i.e., in which the catalyst components were combined substantially simultaneously). For instance, each of Examples 1-2, Examples 3-4, Examples 5-6, Examples 12-13, and Examples 16-17 demonstrate the higher Mw—and higher Mn, higher Mz, and lower HLMI—of polymers produced using the pre-contacting step during catalyst preparation, as compared to preparing the catalyst system by simultaneously combining all of the catalyst components. FIG. 9 summarizes some of these unexpected results for four different alkylaluminum compounds, in which pre-contacting the half-metallocene titanium phosphinimide compound and the alkylaluminum compound significantly increased the Mw (by from 33% to over 100%).

FIG. 10 summarizes data from Table II and FIGS. 1-8, and illustrates the surprising impact of the selection of the alkylaluminum compound on the ratio of Mw/Mn (a measure of the breadth of the molecular weight distribution) of the polymer produced, with or without a pre-contacting step. Using TEA resulted in the narrowest molecular weight distribution (Mw/Mn˜3), while TMA gave a broader molecular weight distribution (Mw/Mn˜5), and TOA resulted in an even broader molecular weight distribution (Mw/Mn˜6-8), and TIBA gave the broadest molecular weight distribution (Mw/Mn˜8-11).

The Journal of Organometallic Chemistry, 263 (1984) 267-271, incorporated herein by reference in its entirety, lists the solubility parameters for certain alkylaluminum compounds (in units of cal^(1/2) cm^(−3/2)): TEA (11.61), TMA (10.18), and TIBA (7.66). Interestingly, as shown by the data in FIG. 10, the Mw/Mn of the polymer increased as the solubility parameter of the alkylaluminum compound decreased.

Thus, it was unexpectedly found—for the catalyst compositions disclosed herein and their use in olefin polymerizations—that molecular weight distribution (Mw/Mn) can be tailored based on the selection of the alkylaluminum compound (and its solubility parameter), and the use of a pre-contacting step (or not) during catalyst preparation can be used to tailor the Mw of the polymer.

TABLE I Examples 1-17 - Polymerization Conditions Half- Pre- Metal- contact Activator H₂ Ti Ex. locene step Activator (g) Al(R^(z))₃ (ppm) activity 1 MET-1 No FSCA 0.101 TIBA 125 366,000 2 MET-1 Yes FSCA 0.104 TIBA 125 348,000 3 MET-1 No FSCA 0.094 TEA 125 279,000 4 MET-1 Yes FSCA 0.111 TEA 125 255,000 5 MET-1 No FSCA 0.105 TMA 125 177,000 6 MET-1 Yes FSCA 0.113 TMA 125 186,000 7 MET-1 Yes FSCA 0.108 DEAC 125 0 8 MET-1 No Borane N/A TIBA 125 204,000 9 MET-1 No Borane N/A TIBA 250 83,000 10 MET-1 Yes Borane N/A TIBA 250 192,000 11 MET-1 — FSCA 0.110 TEA 125 24,000 12 MET-2 No FSCA 0.106 TEA 150 78,000 13 MET-2 Yes FSCA 0.105 TEA 150 72,000 14 MET-3 No FSCA 0.095 TEA 125 378,000 15 MET-3 Yes FSCA 0.091 TEA 125 354,000 16 MET-1 No FSCA 0.105 TOA 125 384,000 17 MET-1 Yes FSCA 0.100 TOA 125 309,000

TABLE II Examples 1-17 - Polymer Properties MI HLMI Mn/1000 Mw/1000 Mz/1000 Ex. (g/10 min) (g/10 min) (g/mol) (g/mol) (g/mol) Mw/Mn 1 0.9 41.9 20.7 181.9 960 8.79 2 0 0.3 43.1 461.9 1399 10.71 3 1.0 26.5 40.1 132.1 314 3.29 4 0 1.3 85.8 261.9 547 3.05 5 5.3 169.6 19.8 104.9 606 5.30 6 2.2 78.6 25.4 140.2 669 5.53 7 — — — — — — 8 0 0 57.3 700.2 1947 12.23 9 0 1.8 26.8 390.6 2181 14.56 10 0.5 54.1 20.5 175.8 1119 8.58 11 — — — — — — 12 0 0.4 84.1 389.3 1127 4.63 13 0 0.1 139.4 657.1 1871 4.72 14 4.0 104.4 22.6 103.1 277 4.56 15 6.4 161.2 18.9 86.2 227 4.57 16 0.2 13.3 25.5 202.6 752 7.94 17 0 2.4 42.9 294.8 1092 6.86

The invention is described above with reference to numerous aspects and specific examples. Many variations will suggest themselves to those skilled in the art in light of the above detailed description. All such obvious variations are within the full intended scope of the appended claims. Other aspects of the invention can include, but are not limited to, the following (aspects are described as “comprising” but, alternatively, can “consist essentially of” or “consist of”):

Aspect 1. An olefin polymerization process, the process comprising:

(i) contacting a half-metallocene titanium phosphinimide compound and an alkylaluminum compound for a first period of time to form a precontacted mixture;

(ii) contacting the precontacted mixture with an activator and an optional co-catalyst for a second period of time to form a catalyst composition; and

(iii) contacting the catalyst composition with an olefin monomer and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce an olefin polymer.

Aspect 2. The process defined in aspect 1, wherein a Mw of the olefin polymer produced by the process is greater (by any amount disclosed herein, e.g., at least about 5%, at least about 10%, at least about 15%, etc.) than the Mw of an olefin polymer produced under the same polymerization conditions using a catalyst system obtained by simultaneously combining the half-metallocene titanium phosphinimide compound, the alkylaluminum compound, the activator, and the optional co-catalyst.

Aspect 3. The process defined in aspect 1 or 2, wherein the half-metallocene titanium phosphinimide compound has the formula:

(B); wherein:

X¹ and X² independently are any halide disclosed herein;

R¹, R², and R³ independently are H or any halide, C₁ to C₃₆ hydrocarbyl group, C₁ to C₃₆ halogenated hydrocarbyl group, C₁ to C₃₆ hydrocarboxy group, or C₁ to C₃₆ hydrocarbylsilyl group disclosed herein; and

Cp is any substituted or unsubstituted cyclopentadienyl, indenyl, or fluorenyl group disclosed herein.

Aspect 4. The process defined in aspect 3, wherein Cp is unsubstituted.

Aspect 5. The process defined in aspect 3, wherein Cp is substituted with any suitable substituent, any suitable number of substituents, and at any suitable position(s) that conforms to the rules of chemical valence.

Aspect 6. The process defined in aspect 3, wherein Cp is substituted, and each substituent independently is any substituent disclosed herein, e.g., H, a halide, a C₁ to C₃₆ hydrocarbyl group, a C₁ to C₃₆ halogenated hydrocarbyl group, a C₁ to C₃₆ hydrocarboxy group, or a C₁ to C₃₆ hydrocarbylsilyl group.

Aspect 7. The process defined in aspect 3, wherein Cp is substituted, and each substituent independently is H or a C₁ to C₁₂ hydrocarbyl group.

Aspect 8. The process defined in aspect 3, wherein Cp is an unsubstituted indenyl group.

Aspect 9. The process defined in any one of aspects 3-8, wherein X¹ and X² are Cl.

Aspect 10. The process defined in any one of aspects 3-9, wherein R¹, R², and R³ independently are H or a C₁ to C₁₈ hydrocarbyl group.

Aspect 11. The process defined in any one of aspects 3-9, wherein R¹, R², and R³ independently are H, Cl, CF₃, a methyl group, an ethyl group, a propyl group, a butyl group (e.g., t-Bu), a pentyl group, a hexyl group, a heptyl group, an octyl group, a nonyl group, a decyl group, an ethenyl group, a propenyl group, a butenyl group, a pentenyl group, a hexenyl group, a heptenyl group, an octenyl group, a nonenyl group, a decenyl group, a phenyl group, a 2,6-diisopropylphenyl group, a tolyl group, a benzyl group, a naphthyl group, a trimethylsilyl group, a triisopropylsilyl group, a triphenylsilyl group, or an allyldimethylsilyl group.

Aspect 12. The process defined in any one of aspects 3-11, wherein at least one of R¹, R², and R³ is a C₃ to C₁₂ alkenyl group.

Aspect 13. The process defined in any one of aspects 3-11, wherein R¹, R², and R³ independently are a C₁ to C₈ alkyl group.

Aspect 14. The process defined in any one of aspects 1-13, wherein the alkylaluminum compound comprises any alkylaluminum compound disclosed herein, e.g., trimethylaluminum, triethylaluminum, triisobutylaluminum, etc., or combinations thereof.

Aspect 15. The process defined in any one of aspects 1-13, wherein the alkylaluminum compound has the formula Al(R^(Z))₃, wherein each R^(Z) independently is any C₁ to C₁₀ alkyl group disclosed herein.

Aspect 16. The process defined in aspect 15, wherein each R^(Z) independently is a C₁ to C₈ alkyl group, or a C₁ to C₄ alkyl group.

Aspect 17. The process defined in aspect 15, wherein each R^(Z) independently is a methyl group, an ethyl group, a propyl group, a n-butyl group, an isobutyl group, or a hexyl group.

Aspect 18. The process defined in any one of the preceding aspects, wherein the first period of time is any suitable time period or in any range of first time periods disclosed herein, e.g., from about 15 minutes to about 48 hours, from about 30 minutes to about 36 hours, from about 1 hour to about 30 hours, etc.

Aspect 19. The process defined in any one of the preceding aspects, wherein the second period of time is any suitable time period or in any range of second time periods disclosed herein, e.g., from about 1 second to about 48 hours, from about 1 minute to about 6 hours, at least about 5 minutes, at least about 10 minutes, etc.

Aspect 20. The process defined in any one of the preceding aspects, wherein the molar ratio (Al:Ti) of the alkylaluminum compound to the half-metallocene titanium phosphinimide compound is any suitable molar ratio or a molar ratio in any range disclosed herein, e.g., from about 0.9:1 to about 10:1, from about 1:1 to about 5:1, from about 1.1:1 to about 2:1, equal to about 1:1, etc.

Aspect 21. The process defined in any one of aspects 1-20, wherein the activator comprises an aluminoxane compound, an organoboron or organoborate compound, an ionizing ionic compound, or any combination thereof.

Aspect 22. The process defined in any one of aspects 1-20, wherein the activator comprises an aluminoxane compound.

Aspect 23. The process defined in any one of aspects 1-20, wherein the activator comprises an organoboron or organoborate compound.

Aspect 24. The process defined in any one of aspects 1-20, wherein the activator comprises an ionizing ionic compound.

Aspect 25. The process defined in any one of aspects 1-20, wherein the activator comprises an activator-support, the activator-support comprising any solid oxide treated with any electron-withdrawing anion disclosed herein.

Aspect 26. The process defined in aspect 25, wherein the solid oxide comprises any solid oxide disclosed herein, e.g., silica, alumina, silica-alumina, silica-coated alumina, aluminum phosphate, aluminophosphate, heteropolytungstate, titania, zirconia, magnesia, boria, zinc oxide, a mixed oxide thereof, or any mixture thereof and the electron-withdrawing anion comprises any electron-withdrawing anion disclosed herein, e.g., sulfate, bisulfate, fluoride, chloride, bromide, iodide, fluorosulfate, fluoroborate, phosphate, fluorophosphate, trifluoroacetate, triflate, fluorozirconate, fluorotitanate, phospho-tungstate, or any combination thereof.

Aspect 27. The process defined in aspect 25, wherein the activator-support comprises fluorided alumina, chlorided alumina, bromided alumina, sulfated alumina, fluorided silica-alumina, chlorided silica-alumina, bromided silica-alumina, sulfated silica-alumina, fluorided silica-zirconia, chlorided silica-zirconia, bromided silica-zirconia, sulfated silica-zirconia, fluorided silica-titania, fluorided-chlorided silica-coated alumina, fluorided silica-coated alumina, sulfated silica-coated alumina, phosphated silica-coated alumina, or any combination thereof.

Aspect 28. The process defined in aspect 25, wherein the activator-support comprises fluorided alumina, sulfated alumina, fluorided silica-alumina, sulfated silica-alumina, fluorided silica-coated alumina, fluorided-chlorided silica-coated alumina, sulfated silica-coated alumina, or any combination thereof.

Aspect 29. The process defined in aspect 25, wherein the activator-support comprises a fluorided solid oxide, a sulfated solid oxide, or any combination thereof.

Aspect 30. The process defined in any one of the preceding aspects, wherein step (ii) comprises contacting the precontacted mixture with the activator and the co-catalyst, e.g., any co-catalyst disclosed herein.

Aspect 31. The process defined in aspect 30, wherein the co-catalyst comprises an organoaluminum compound, an organozinc compound, an organomagnesium compound, an organolithium compound, or any combination thereof.

Aspect 32. The process defined in aspect 30, wherein the co-catalyst comprises an organoaluminum compound.

Aspect 33. The process defined in aspect 30, wherein the co-catalyst comprises an aluminoxane compound, an organoboron or organoborate compound, an ionizing ionic compound, an organoaluminum compound, an organozinc compound, an organomagnesium compound, an organolithium compound, or any combination thereof.

Aspect 34. The process defined in any one of aspects 1-20 and 25-32, wherein the catalyst composition is substantially free of aluminoxane compounds, organoboron or organoborate compounds, ionizing ionic compounds, or combinations thereof.

Aspect 35. The process defined in any one of the preceding aspects, wherein a catalyst activity of the catalyst composition is in any range disclosed herein, e.g., greater than about 20,000 grams, greater than about 50,000 grams, greater than about 100,000 grams, etc., of ethylene polymer per gram of the half-metallocene titanium phosphinimide compound per hour, under slurry polymerization conditions, with a triisobutylaluminum co-catalyst, using isobutane as a diluent, and with a polymerization temperature of 80° C. and a reactor pressure of 340 psig.

Aspect 36. The process defined in any one of the preceding aspects, wherein the weight ratio of the half-metallocene titanium phosphinimide compound to the activator (e.g., activator-support) is in any range of weight ratios disclosed herein, e.g., from about 1:1 to about 1:1,000,000, from about 1:10 to about 1:10,000, from about 1:20 to about 1:1000, etc.

Aspect 37. The composition defined in any one of the preceding aspects, wherein the weight ratio of the activator (e.g., activator-support) to the alkylaluminum compound and co-catalyst (if used) is in any range of weight ratios disclosed herein, e.g., from about 1:5 to about 1000:1, from about 1:3 to about 200:1, from about 1:1 to about 100:1, etc.

Aspect 38. The process defined in any one of the preceding aspects, wherein the olefin monomer comprises any olefin monomer disclosed herein, e.g., any C₂-C₂₀ olefin.

Aspect 39. The process defined in any one of the preceding aspects, wherein the olefin monomer and the optional olefin comonomer independently comprise a C₂-C₂₀ alpha-olefin.

Aspect 40. The process defined in any one of the preceding aspects, wherein the olefin monomer comprises ethylene.

Aspect 41. The process defined in any one of the preceding aspects, wherein the catalyst composition is contacted with ethylene and an olefin comonomer comprising a C₃-C₁₀ alpha-olefin.

Aspect 42. The process defined in any one of the preceding aspects, wherein the catalyst composition is contacted with ethylene and an olefin comonomer comprising 1-butene, 1-hexene, 1-octene, or a mixture thereof.

Aspect 43. The process defined in any one of aspects 1-39, wherein the olefin monomer comprises propylene.

Aspect 44. The process defined in any one of the preceding aspects, wherein the polymerization reactor system comprises a batch reactor, a slurry reactor, a gas-phase reactor, a solution reactor, a high pressure reactor, a tubular reactor, an autoclave reactor, or a combination thereof.

Aspect 45. The process defined in any one of the preceding aspects, wherein the polymerization reactor system comprises a slurry reactor, a gas-phase reactor, a solution reactor, or a combination thereof.

Aspect 46. The process defined in any one of the preceding aspects, wherein the polymerization reactor system comprises a loop slurry reactor.

Aspect 47. The process defined in any one of aspects 1-46, wherein the polymerization reactor system comprises a single reactor.

Aspect 48. The process defined in any one of aspects 1-46, wherein the polymerization reactor system comprises 2 reactors.

Aspect 49. The process defined in any one of aspects 1-46, wherein the polymerization reactor system comprises more than 2 reactors.

Aspect 50. The process defined in any one of the preceding aspects, wherein the olefin polymer comprises any olefin polymer disclosed herein.

Aspect 51. The process defined in any one of aspects 1-40, wherein the olefin polymer comprises an ethylene homopolymer, an ethylene/1-butene copolymer, an ethylene/1-hexene copolymer, or an ethylene/1-octene copolymer.

Aspect 52. The process defined in any one of aspects 1-40, wherein the olefin polymer comprises an ethylene/1-hexene copolymer.

Aspect 53. The process defined in any one of aspects 1-39, wherein the olefin polymer comprises a polypropylene homopolymer or a propylene-based copolymer.

Aspect 54. The process defined in any one of aspects 1-53, wherein the polymerization conditions comprise a polymerization reaction temperature in a range from about 60° C. to about 120° C. and a reaction pressure in a range from about 200 to about 1000 psig (about 1.4 to about 6.9 MPa).

Aspect 55. The process defined in any one of aspects 1-54, wherein the polymerization conditions are substantially constant, e.g., for a particular polymer grade.

Aspect 56. The process defined in any one of aspects 1-55, wherein no hydrogen is added to the polymerization reactor system.

Aspect 57. The process defined in any one of aspects 1-55, wherein hydrogen is added to the polymerization reactor system.

Aspect 58. The process defined in any one of the preceding aspects, wherein the olefin polymer has a density in any range disclosed herein, e.g., from about 0.87 to about 0.96, from about 0.87 to about 0.94, from about 0.88 to about 0.93, from about 0.89 to about 0.93, from about 0.93 to about 0.96, from about 0.90 to about 0.92 g/cm³, etc.

Aspect 59. The process defined in any one of the preceding aspects, wherein the olefin polymer has a ratio of Mw/Mn in any range disclosed herein, e.g., from about 2 to about 18, from about 2.5 to about 15, from about 3 to about 15, from about 3 to about 12, etc.

Aspect 60. The process defined in any one of the preceding aspects, wherein the olefin polymer has a Mw in any range disclosed herein, e.g., from about 50,000 to about 750,000, from about 60,000 to about 600,000, from about 70,000 to about 500,000 g/mol, etc.

Aspect 61. The process defined in any one of the preceding aspects, wherein the olefin polymer has a Mn in any range disclosed herein, e.g., from about 10,000 to about 100,000, from about 12,000 to about 100,000, from about 14,000 to about 90,000 g/mol, etc.

Aspect 62. The process defined in any one of the preceding aspects, wherein the olefin polymer has a ratio of Mz/Mw in any range disclosed herein, e.g., from about 1.8 to about 10, from about 2 to about 9, from about 2 to about 8, etc.

Aspect 63. The process defined in any one of the preceding aspects, wherein the olefin polymer has a Mz in any range disclosed herein, e.g., from about 300,000 to about 1,500,000, from about 500,000 to about 1,500,000, from about 500,000 to about 1,000,000, from about 500,000 to about 1,000,000 g/mol, etc.

Aspect 64. The process defined in any one of the preceding aspects, wherein the olefin polymer has a HLMI in any range disclosed herein, e.g., less than about 200, less than about 100, less than about 50, less than about 25, from about 1 to about 200, from about 1 to about 100 g/10 min, etc.

Aspect 65. The process defined in any one of the preceding aspects, wherein the olefin polymer has a unimodal molecular weight distribution.

Aspect 66. An olefin polymer (e.g., an ethylene homopolymer or copolymer) produced by the olefin polymerization process defined in any one of the preceding aspects.

Aspect 67. An article comprising the olefin polymer defined in aspect 66.

Aspect 68. A method or forming or preparing an article of manufacture comprising an olefin polymer, the method comprising (I) performing the olefin polymerization process defined in any one of aspects 1-65 to produce an olefin polymer, and (II) forming the article of manufacture comprising the olefin polymer, e.g., via any technique disclosed herein.

Aspect 69. The article defined in any one of aspects 67-68, wherein the article is an agricultural film, an automobile part, a bottle, a drum, a fiber or fabric, a food packaging film or container, a food service article, a fuel tank, a geomembrane, a household container, a liner, a molded product, a medical device or material, a pipe, a sheet or tape, or a toy.

Aspect 70. A process for producing an ethylene polymer with a target ratio of Mw/Mn, the process comprising:

(a) selecting an alkylaluminum compound based on a solubility parameter of the alkylaluminum compound; and

(b) contacting a catalyst composition with ethylene and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce the ethylene polymer with the target ratio of Mw/Mn;

wherein the catalyst composition comprises a half-metallocene titanium phosphinimide compound, an activator, and the alkylaluminum compound.

Aspect 71. A process for controlling a ratio of Mw/Mn of an ethylene polymer, the process comprising:

(A) contacting a catalyst composition with ethylene and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce the ethylene polymer,

wherein the catalyst composition comprises a half-metallocene titanium phosphinimide compound, an activator, and an alkylaluminum compound; and

(B) adjusting a solubility parameter of the alkylaluminum compound to control the ratio of Mw/Mn of the ethylene polymer.

Aspect 72. The process defined in aspect 70 or 71, wherein Mw/Mn increases as the solubility parameter decreases.

Aspect 73. The process defined in any one of aspects 70-72, wherein the ratio of Mw/Mn is less than or equal to about 6, and the alkylaluminum compound comprises trimethylaluminum, triethylaluminum, or a combination thereof.

Aspect 74. The process defined in aspect 73, wherein the ethylene polymer has a ratio of Mw/Mn in any range disclosed herein, e.g., from about 2.5 to about 6, from about 2.5 to about 5.5, from about 3 to about 6, from about 3 to about 5.5, etc.

Aspect 75. The process defined in any one of aspects 70-72, wherein the ratio of Mw/Mn is greater than or equal to about 6, and the alkylaluminum compound comprises triisobutylaluminum, trioctylaluminum, or a combination thereof.

Aspect 76. The process defined in aspect 75, wherein the ethylene polymer has a ratio of Mw/Mn in any range disclosed herein, e.g., from about 6 to about 18, from about 6.5 to about 15, from about 7 to about 17, etc. 

We claim:
 1. An olefin polymerization process, the process comprising: (i) contacting a half-metallocene titanium phosphinimide compound and an alkylaluminum compound for a first period of time to form a precontacted mixture; (ii) contacting the precontacted mixture with an activator and an optional co-catalyst for a second period of time to form a catalyst composition; and (iii) contacting the catalyst composition with an olefin monomer and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce an olefin polymer; wherein: a Mw of the olefin polymer produced by the process is greater than the Mw of an olefin polymer produced under the same polymerization conditions using a catalyst system obtained by simultaneously combining the half-metallocene titanium phosphinimide compound, the alkylaluminum compound, the activator, and the optional co-catalyst.
 2. The process of claim 1, wherein the alkylaluminum compound comprises trimethylaluminum, triethylaluminum, triisobutylaluminum, tri-n-octylaluminum, or any combination thereof.
 3. The process of claim 1, wherein the half-metallocene titanium phosphinimide compound has the formula:

(B); wherein: X¹ and X² independently are a halide; R¹, R², and R³ independently are H or a halide, C₁ to C₃₆ hydrocarbyl group, C₁ to C₃₆ halogenated hydrocarbyl group, C₁ to C₃₆ hydrocarboxy group, or C₁ to C₃₆ hydrocarbylsilyl group; and Cp is a substituted or unsubstituted cyclopentadienyl, indenyl, or fluorenyl group.
 4. The process of claim 3, wherein: X¹ and X² are Cl; R¹, R², and R³ independently are H or C₁ to C₁₈ hydrocarbyl group; and Cp is an unsubstituted cyclopentadienyl or indenyl group.
 5. The process of claim 1, wherein the first period of time is in a range from about 30 minutes to about 36 hours.
 6. The process of claim 1, wherein the Mw of the olefin polymer produced by the process is at least about 25% greater than the Mw of the olefin polymer produced under the same polymerization conditions using a catalyst system obtained by simultaneously combining the half-metallocene titanium phosphinimide compound, the alkylaluminum compound, the activator, and the optional co-catalyst.
 7. The process of claim 1, wherein the molar ratio of the alkylaluminum compound to the half-metallocene titanium phosphinimide compound in step (i) is in a range from about 1:1 to about 5:1.
 8. The process of claim 1, wherein the activator comprises an aluminoxane compound, an organoboron or organoborate compound, an ionizing ionic compound, or any combination thereof.
 9. The process of claim 1, wherein the activator comprises an activator-support, the activator-support comprising a solid oxide treated with an electron-withdrawing anion.
 10. The process of claim 1, wherein: the polymerization reactor system comprises a slurry reactor, gas-phase reactor, solution reactor, or a combination thereof, and the catalyst composition is contacted with ethylene and an olefin comonomer comprising 1-butene, 1-hexene, 1-octene, or a mixture thereof.
 11. The process of claim 10, wherein: the precontacted mixture is contacted with the activator and an organoaluminum co-catalyst in step (ii); and the activator comprises a fluorided solid oxide and/or a sulfated solid oxide.
 12. The process of claim 1, wherein: the olefin polymer comprises an ethylene homopolymer and/or an ethylene/α-olefin copolymer; the activator comprises an activator-support, an aluminoxane compound, an organoboron or organoborate compound, an ionizing ionic compound, or any combination thereof; and the Mw of the olefin polymer produced by the process is at least about 25% greater than the Mw of the olefin polymer produced under the same polymerization conditions using a catalyst system obtained by simultaneously combining the half-metallocene titanium phosphinimide compound, the alkylaluminum compound, the activator, and the optional co-catalyst.
 13. A process for producing an ethylene polymer with a target ratio of Mw/Mn, the process comprising: (a) selecting an alkylaluminum compound based on a solubility parameter of the alkylaluminum compound; and (b) contacting a catalyst composition with ethylene and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce the ethylene polymer with the target ratio of Mw/Mn; wherein the catalyst composition comprises a half-metallocene titanium phosphinimide compound, an activator, and the alkylaluminum compound.
 14. The process of claim 13, wherein: the alkylaluminum compound comprises trimethylaluminum, triethylaluminum, or a combination thereof; and the target ratio of Mw/Mn is in a range from about 2.5 to about
 6. 15. The process of claim 13, wherein: Mw/Mn increases as the solubility parameter decreases; and the polymerization reactor system comprises a slurry reactor, gas-phase reactor, solution reactor, or a combination thereof.
 16. The process of claim 13, wherein the ethylene polymer comprises an ethylene homopolymer, an ethylene/1-butene copolymer, an ethylene/1-hexene copolymer, an ethylene/1-octene copolymer, or any combination thereof; the activator comprises an activator-support, an aluminoxane compound, an organoboron or organoborate compound, an ionizing ionic compound, or any combination thereof; and the half-metallocene titanium phosphinimide compound has the formula:

(B); wherein: X¹ and X² independently are a halide; R¹, R², and R³ independently are H or a halide, C₁ to C₃₆ hydrocarbyl group, C₁ to C₃₆ halogenated hydrocarbyl group, C₁ to C₃₆ hydrocarboxy group, or C₁ to C₃₆ hydrocarbylsilyl group; and Cp is a substituted or unsubstituted cyclopentadienyl, indenyl, or fluorenyl group.
 17. A process for controlling a ratio of Mw/Mn of an ethylene polymer, the process comprising: (A) contacting a catalyst composition with ethylene and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce the ethylene polymer, wherein the catalyst composition comprises a half-metallocene titanium phosphinimide compound, an activator, and an alkylaluminum compound; and (B) adjusting a solubility parameter of the alkylaluminum compound to control the ratio of Mw/Mn of the ethylene polymer.
 18. The process of claim 17, wherein Mw/Mn increases as the solubility parameter decreases.
 19. The process of claim 17, wherein: the alkylaluminum compound comprises trimethylaluminum, triethylaluminum, or a combination thereof; and the ratio of Mw/Mn of the ethylene polymer is in a range from about 2.5 to about
 6. 20. The process of claim 17, wherein: the alkylaluminum compound comprises triisobutylaluminum, trioctylaluminum, or a combination thereof; and the ratio of Mw/Mn of the ethylene polymer is in a range from about 6.5 to about
 15. 